Lewis Base Catalysts and Methods Thereof

ABSTRACT

The present disclosure relates to Lewis base catalysts. Catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, or copolymerization as the Lewis base catalysts (e.g., bis(aryl phenolate) five-membered ring catalysts), can be stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers having high molecular weights or polymers having low to very molecular weights, and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts. Hence, the present disclosure demonstrates highly active catalysts capable of operating at high reactor temperatures while producing polymers with controlled molecular weights and or robust isotacticity.

PRIORITY

This invention claims priority to and the benefit of U.S. Ser. No. 62/804,389, filed Feb. 12, 2019, which is incorporated by reference herein.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is also related to the following:

1) concurrently filed U.S. Ser. No. ______, entitled “Lewis Base Catalysts and Methods Thereof” (attorney docket number 2019EM041), which claims priority to 62/804,353, filed Feb. 12, 2019; 2) concurrently filed U.S. Ser. No. ______, entitled “Bis(Aryl Phenolate) Lewis Base Catalysts and Methods Thereof” (attorney docket number 2019EM043), which claims priority to 62/804,372, filed Feb. 12, 2019; 3) concurrently filed U.S. Ser. No. ______, entitled “Transition Metal Bis(Phenolate) Complexes and Their Use as Catalysts for Olefin Polymerization” (attorney docket number 2020EM045), which claims priority to 62/804,372, filed Feb. 12, 2019; 4) concurrently filed U.S. Ser. No. ______, entitled “Supported Transition Metal Bis(Phenolate) Complexes and Their Use as Catalysts for Olefin Polymerization” (attorney docket number 2020EM046), which claims priority to 62/804,372, filed Feb. 12, 2019; 5) concurrently filed U.S. Ser. No. ______ entitled “Propylene Copolymers Obtained Using Transition Metal Bis(Phenolate) Catalyst Complexes and Homogeneous Process for Production Thereof” (attorney docket number 2020EM048); 6) concurrently filed U.S. Ser. No. ______ entitled “Propylene Polymers Obtained Using Transition Metal Bis(Phenolate) Catalyst Complexes and Homogeneous Process for Production Thereof” (attorney docket number 2020EM049); 7) concurrently filed U.S. Ser. No. ______ entitled “Ethylene-Alpha-Olefin-Diene Monomer Copolymers Obtained Using Transition Metal Bis(Phenolate) Catalyst Complexes and Homogeneous Process for Production Thereof” (attorney docket number 2020EM050); and 8) concurrently filed U.S. Ser. No. ______ entitled “Polyethylene Compositions Obtained Using Transition Metal Bis(Phenolate) Catalyst Complexes and Homogeneous Process for Production Thereof” (attorney docket number 2020EM051).

FIELD

The present disclosure relates to Lewis base transition metal complexes, catalyst systems including Lewis base transition metal complexes, and polymerization processes to produce polyolefin polymers such as ethylene based polymers and propylene based polymers.

BACKGROUND

Olefin polymerization catalysts are of great use in industry and polyolefins are widely used commercially because of their robust physical properties. Hence, there is interest in finding new catalyst systems that increase the marketing value of the catalyst and allow the production of polymers having improved properties. The physical properties (such as transition temperature, viscosity, etc.) and mechanical properties (such as strength, stiffness, and toughness) depend on the molecular weight of the polymer.

Low molecular weight polyolefins, such as low-density polyethylene (LDPE) or ultra-low-molecular-weight polyethylene (PE-WAX), are among the most versatile products in the chemical industry, useful in diverse products and applications, and widely used in hot-melt adhesives, as well as plasticizers, or for waxes and wax additives production. However, challenges remain for the development of highly active catalysts capable of operating at high reactor temperatures for the production of controllable molecular weight polyolefins of interest. On the other hand, polyolefins with high molecular weight, such as high-molecular-weight polyethylene (HMWPE) or ultra-high-molecular-weight polyethylene (UHMWPE), generally have valuable mechanical properties.

Additionally, pre-catalysts (neutral, unactivated complexes) should be thermally stable at and above ambient temperature, as they are often stored for weeks before being used. The performance of a given catalyst is closely influenced by the reaction conditions, such as the monomer concentrations and temperature. From this stance, the solution process, which benefits from being run at temperatures above 120° C., is particularly challenging for catalyst development. At such high reactor temperatures, it is often difficult to maintain high catalyst activity and high molecular weight capability as both attributes quite consistently decline with an increase of reactor temperature. With a wide range of polyolefin products desired, from high density polyethylene (HDPE) to elastomers (e.g., thermoplastic elastomers (TPE); ethylene-propylene-diene (EPDM)), many different catalyst systems may be needed, as it is unlikely that a single catalyst will be able to address all the needs for the production of these various polyolefin products. The strict set of requirements needed for the development and production of new polyolefin products makes the identification of suitable catalysts for a given product and production process a highly challenging endeavor.

There is a need for new and improved catalysts, catalyst systems, and processes for the polymerization of olefins in order to achieve polymer properties such as narrow polydispersity indices, while controlling the molecular weight of the polymer (e.g., high molecular weight or low molecular weight according to the demand). Furthermore, there is still a need to develop highly active catalysts capable of operating at high reactor temperatures (e.g., catalysts with high stability and good activity at high polymerization temperatures) while producing polymers with controlled molecular weights. In the case of polypropylenes, there is further a need for catalysts and processes that provide isotactic polypropylenes having one or more of the aforementioned properties.

References for citing in an Information Disclosure Statement (37 CFR 1.97(h)): U.S. Pat. No. 7,030,256; Baier, M. et al. (2014) “Post-Metallocenes in the Industrial Production of Poly-Plefins,” Angew. Chem. Int. Ed., v. 53, pp. 9722-9744; KR 2018/022137; WO 2016/172110.

SUMMARY

The present disclosure relates to catalyst compounds represented by Formula (I):

wherein:

M is a group 3, 4, or 5 metal;

each A¹, A², A³, and A⁴ is independently an aromatic group;

J is a heterocyclic Lewis base;

each Q¹ and Q² are independently selected from O, S, N(R³⁰), or P(R³⁰), wherein R³⁰ is C₁-C₄₀ hydrocarbyl, substituted C₁-C₄₀ hydrocarbyl, or a heteroatom, or a heteroatom-containing group;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand,

wherein the ring formed by M, Q¹, A³, A¹, and J is an eight-membered ring and the ring formed by M, Q², A⁴, A² and, J is an eight-membered ring.

In yet another embodiment, the present disclosure provides a catalyst system comprising an activator and a catalyst of the present disclosure.

In yet another embodiment, the present disclosure provides a catalyst system comprising an activator and a catalyst of the present disclosure.

In still another embodiment, the present disclosure provides a polymerization process comprising a) contacting one or more olefin monomers with a catalyst system comprising: i) an activator and ii) a catalyst of the present disclosure.

In still another embodiment, the present disclosure provides a polyolefin formed by a catalyst system and or method of the present disclosure.

In another class of embodiments, the present disclosure provides for a process for the production of an ethylene alpha-olefin copolymer comprising polymerizing ethylene and at least one C₃-C₂₀ alpha-olefin by contacting the ethylene and the at least one C₃-C₂₀ alpha-olefin with a catalyst system in at least one continuous stirred tank reactor or loop reactor.

In another class of embodiments, the present disclosure provides for a process for the production of a propylene alpha-olefin copolymer comprising polymerizing propylene and at least one ethylene and/or C₄-C₂₀ alpha-olefin by contacting the propylene and the at least one ethylene and/or at least one C₄-C₂₀ alpha-olefin with a catalyst system in at least one continuous stirred tank reactor or loop reactor.

In at least one embodiment the catalyst compounds represented by Formula (I) feature two eight-membered metallocycle rings. The first of these eight-membered metallocycle rings contains the atoms from the metal M, a heteroatom (e.g., oxygen, such as phenolate oxygen), two carbons of the aryl group A³, two atoms of the aryl group A¹, and two atoms from the bridging Lewis base group J. The second of these eight-membered metallocycle rings contains the atoms from the metal M, a heteroatom, two carbons of the aryl group A⁴, two atoms of the aryl group A², and two atoms from the bridging Lewis base group J.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is an image of the X-Ray crystallographic structure of a catalyst as determined by single-crystal X-ray diffraction, according to one embodiment.

FIG. 2 is an illustration of the bis(arylphenolate) ligand.

DETAILED DESCRIPTION

The present disclosure provides catalyst compounds including a Lewis base tridentate ligand, such as a bis(arylphenolate) five-membered ring tridentate ligand, which coordinates to a transition metal center, forming two eight-membered rings, catalyst systems including such catalyst compounds, and uses thereof. In at least one embodiment, the Lewis base is a heterocyclic ring having 5 ring atoms which may include at least two heteroatoms, such as at least one of which is a nitrogen, in a way that the heteroatoms can be located in position 1 and position 3 of the heterocyclic ring. The five-membered ring heterocycles can be azoles, for example.

Catalyst compounds of the present disclosure can be zirconium or hafnium-containing compounds having one or more aryl and/or heteroaryl ligand(s) substituted and linked with a Lewis base. In another class of embodiments, the present disclosure is directed to polymerization processes to produce polyolefin polymers from catalyst systems including one or more olefin polymerization catalysts, at least one activator, and an optional support. Polyolefin polymers can be polyethylene polymers or polypropylene polymers.

The Lewis base tridentate ligand is a class of tridentate ligands that may use heterocycles such as an azole group. This class of ligands can include bis(arylphenolate)heterocycles or bis(arylphenolate) heterocyclic ligands. These ligands coordinate to a transition metal in a “tridentate” fashion, which means that the ligand forms three different bonds to the metal center. A feature of the bis(arylphenolate)heterocycle complexes, for example, is that the ligand binds in a tridentate fashion with the formation of two eight-membered metallocycle rings. With the ligand coordinated to the metal in this fashion, the complex is thought to be chiral (i.e., lacking a mirror plane of symmetry). Without being bound by theory, it has been discovered that when using these catalysts for the production of polypropylene and other polymers of C₃ and higher alpha olefins, the chirality is advantageous for the production of polyolefins having high isotacticity.

Catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, ethylene alpha-olefin (e.g., ethylene-1-octene) copolymerization, or propylene alpha-olefin copolymerization as the Lewis base catalysts can be stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts, because polymerizations in general occur at a higher rate at higher temperatures. Furthermore, the stable catalysts with good activity can also provide formation of polymers having low molecular weight (e.g., Mw of about 10,500 g/mol or less) to very low molecular weight (e.g., Mw of about 6,000 g/mol or less).

For the purposes of the present disclosure, the numbering scheme for the Periodic Table Groups is used as described in Chemical And Engineering News, v. 63(5), pg. 27 (1985). Therefore, a “group 4 metal” is an element from group 4 of the Periodic Table, e.g., Hf, Ti, or Zr.

The following abbreviations may be used herein: Me is methyl, Et is ethyl, Ph is phenyl, tBu is tertiary butyl, MAO is methylalumoxane, NMR is nuclear magnetic resonance, t is time, s is second, h is hour, psi is pounds per square inch, psig is pounds per square inch gauge, equiv is equivalent, Å is angstroms, RPM is rotation per minute.

The specification describes transition metal complexes. The term complex is used to describe molecules in which an ancillary ligand is coordinated to a central transition metal atom. The ligand is bulky and stably bonded to the transition metal so as to maintain its influence during use of the catalyst, such as polymerization. The ligand may be coordinated to the transition metal by covalent bond and/or electron donation coordination or intermediate bonds. The transition metal complexes are generally subjected to activation to perform their polymerization or oligomerization function using an activator which, without being bound by theory, is believed to create a cation as a result of the removal of an anionic group, often referred to as a leaving group, from the transition metal.

As used herein, “olefin polymerization catalyst(s)” refers to any catalyst, such as an organometallic complex or compound that is capable of coordination polymerization addition where successive monomers are added in a monomer chain at the organometallic active center.

The terms “substituent,” “radical,” “group,” and “moiety” may be used interchangeably.

“Conversion” is the amount of monomer that is converted to polymer product, and is reported as mol % and is calculated based on the polymer yield and the amount of monomer fed into the reactor.

“Catalyst activity” is a measure of how active the catalyst is and is reported as the grams of product polymer (P) produced per millimole of catalyst (cat) used per hour (gP·mmolcat⁻¹·h⁻¹).

The term “heteroatom” refers to any group 13-17 element, excluding carbon. A heteroatom may include B, Si, Ge, Sn, N, P, As, O, S, Se, Te, F, Cl, Br, and I. The term “heteroatom” may include the aforementioned elements with hydrogens attached, such as BH, BH₂, SiH₂, OH, NH, NH₂, etc. The term “substituted heteroatom” describes a heteroatom that has one or more of these hydrogen atoms replaced by a hydrocarbyl or substituted hydrocarbyl group(s).

An “olefin,” alternatively referred to as “alkene,” is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond. For purposes of this specification and the claims appended thereto, when a polymer or copolymer is referred to as including an olefin, the olefin present in such polymer or copolymer is the polymerized form of the olefin. For example, when a copolymer is said to have an “ethylene” content of 35 wt % to 55 wt %, it is understood that the mer unit in the copolymer is derived from ethylene in the polymerization reaction and said derived units are present at 35 wt % to 55 wt %, based upon the weight of the copolymer. A “polymer” has two or more of the same or different mer units. A “homopolymer” is a polymer having mer units that are the same. A “copolymer” is a polymer having two or more mer units that are different from each other. A “terpolymer” is a polymer having three mer units that are different from each other. “Different” is used to refer to mer units indicates that the mer units differ from each other by at least one atom or are different isomerically. Accordingly, the definition of copolymer, as used herein, includes terpolymers. An “ethylene polymer” or “ethylene copolymer” is a polymer or copolymer including at least 50 mol % ethylene derived units, a “propylene polymer” or “propylene copolymer” is a polymer or copolymer including at least 50 mol % propylene derived units, and so on. An “ethylene polymer” or “ethylene copolymer” is a polymer or copolymer including at least 50 mol % ethylene derived units, a “propylene polymer” or “propylene copolymer” is a polymer or copolymer including at least 50 mol % propylene derived units, and so on.

The term “alpha-olefin” refers to an olefin having a terminal carbon-to-carbon double bond in the structure thereof ((R¹R²)—C═CH₂, where R¹ and R² can be independently hydrogen or any hydrocarbyl group; such as R¹ is hydrogen and R² is an alkyl group). A “linear alpha-olefin” is an alpha-olefin defined above wherein R¹ is hydrogen, and R² is hydrogen or a linear alkyl group.

For the purposes of the present disclosure, ethylene shall be considered an alpha-olefin.

As used herein, and unless otherwise specified, the term “C_(n)” means hydrocarbon(s) having n carbon atom(s) per molecule, wherein n is a positive integer. The term “hydrocarbon” means a class of compounds containing hydrogen bound to carbon, and encompasses (i) saturated hydrocarbon compounds, (ii) unsaturated hydrocarbon compounds, and (iii) mixtures of hydrocarbon compounds (saturated and/or unsaturated), including mixtures of hydrocarbon compounds having different values of n. Likewise, a “C_(m)-C_(y)” group or compound refers to a group or compound comprising carbon atoms at a total number thereof in the range from m to y. Thus, a C₁-C₅₀ alkyl group refers to an alkyl group comprising carbon atoms at a total number thereof in the range from 1 to 50.

Unless otherwise indicated, (e.g., the definition of “substituted hydrocarbyl”, “substituted aromatic”, etc.), the term “substituted” means that at least one hydrogen atom has been replaced with at least one non-hydrogen group, such as a hydrocarbyl group, a heteroatom, or a heteroatom containing group, such as halogen (such as Br, Cl, F or I) or at least one functional group such as —NR*₂, —OR*, —SeR*, —TeR*, —PR*₂, —AsR*₂, —SbR*₂, —SR*, —BR*₂, —SiR*₃, —GeR*₃, —SnR*₃, —PbR*₃, where each R* is independently a hydrocarbyl or halocarbyl radical, and two or more R* may join together to form a substituted or unsubstituted completely saturated, partially unsaturated, or aromatic cyclic or polycyclic ring structure), or where at least one heteroatom has been inserted within a hydrocarbyl ring.

The term “substituted hydrocarbyl” means a hydrocarbyl radical in which at least one hydrogen atom of the hydrocarbyl radical has been substituted with at least one heteroatom (such as halogen, e.g., Br, Cl, F or I) or heteroatom-containing group (such as a functional group, e.g., —NR*₂, —OR*, —SeR*, —TeR*, —PR*₂, —AsR*₂, —SbR*₂, —SR*, —BR*₂, —SiR*₃, —GeR*₃, —SnR*₃, —PbR*₃, where each R* is independently a hydrocarbyl or halocarbyl radical, and two or more R* may join together to form a substituted or unsubstituted completely saturated, partially unsaturated, or aromatic cyclic or polycyclic ring structure), or where at least one heteroatom has been inserted within a hydrocarbyl ring. The term “hydrocarbyl substituted phenyl” means a phenyl group having 1, 2, 3, 4 or 5 hydrogen groups replaced by a hydrocarbyl or substituted hydrocarbyl group. For example, the “hydrocarbyl substituted phenyl” group can be represented by the formula:

where each of R^(a), R^(b), R^(c), R^(d), and R^(e) can be independently selected from hydrogen, C₁-C₄₀ hydrocarbyl or C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group (provided that at least one of R^(a), R^(b), R^(c), R^(d), and R^(e) is not H), or two or more of R^(a), R^(b), R^(c), R^(d), and R^(e) can be joined together to form a C₄-C₆₂ cyclic or polycyclic hydrocarbyl ring structure, or a combination thereof.

The term “substituted aromatic,” means an aromatic group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted phenyl,” mean a phenyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted carbazole,” means a carbazolyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted naphthyl,” means a naphthyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted anthracenyl,” means an anthracenyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted fluorenyl” means a fluorenyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group.

The term “substituted benzyl” means a benzyl group having 1 or more hydrogen groups replaced by a hydrocarbyl, substituted hydrocarbyl, heteroatom or heteroatom containing group, such as a substituted benzyl group is represented by the formula:

where each of R^(a′), R^(b′), R^(c′), R^(d′), and R^(e′) and Z is independently selected from hydrogen, C₁-C₄₀ hydrocarbyl or C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group (provided that at least one of R^(a′), R^(b′), R^(c′), R^(d′), and R^(e′) and Z is not H), or two or more of R^(a′), R^(b′), R^(c′), R^(d′), and R^(e′) and Z may be joined together to form a C₄-C₆₂ cyclic or polycyclic ring structure, or a combination thereof.

The terms “alkoxy” and “alkoxide” mean an alkyl or aryl group bound to an oxygen atom, such as an alkyl ether or aryl ether group/radical connected to an oxygen atom and can include those where the alkyl/aryl group is a C₁ to C₁₀ hydrocarbyl. The alkyl group may be straight chain, branched, or cyclic. The alkyl group may be saturated or unsaturated. Examples of suitable alkoxy radicals can include methoxy, ethoxy, n-propoxy, iso-propoxy, n-butoxy, iso-butoxy, sec-butoxy, tert-butoxy, phenoxyl.

The term “alkenyl” means a straight-chain, branched-chain, or cyclic hydrocarbon radical having one or more double bonds. These alkenyl radicals may be optionally substituted. Examples of suitable alkenyl radicals can include ethenyl, propentyl, allyl, 1,4-butadienyl cyclopropentyl, cyclobutenyl, cyclopentenyl, cyclohexenyl, cycloctenyl, including their substituted analogues.

The terms “alkyl radical,” and “alkyl” are used interchangeably throughout this disclosure. For purposes of this disclosure, “alkyl radical” is defined to be C₁-C₁₀₀ alkyls that may be linear, branched, or cyclic. Examples of such radicals can include methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, sec-butyl, tert-butyl, pentyl, iso-amyl, hexyl, octyl cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cyclooctyl, including their substituted analogues. Substituted alkyl radicals are radicals in which at least one hydrogen atom of the alkyl radical has been substituted with at least a non-hydrogen group, such as a hydrocarbyl group, a heteroatom, or a heteroatom containing group, such as halogen (such as Br, Cl, F or I) or at least one functional group such as —NR*₂, —OR*, —SeR*, —TeR*, —PR*₂, —AsR*₂, —SbR*₂, —SR*, —BR*₂, —SiR*₃, —GeR*₃, —SnR*₃, or —PbR*₃, and each R* is independently a hydrocarbyl or halocarbyl radical, and two or more R* may join together to form a substituted or unsubstituted completely saturated, partially unsaturated, or aromatic cyclic or polycyclic ring structure), or where at least one heteroatom has been inserted within a hydrocarbyl ring.

The term “aryl” or “aryl group” means an aromatic ring and the substituted variants thereof, such as phenyl, 2-methyl-phenyl, xylyl, 4-bromo-xylyl. Likewise, heteroaryl means an aryl group where a ring carbon atom (or two or three ring carbon atoms) has been replaced with a heteroatom, such as N, O, or S. As used herein, the term “aromatic” also refers to pseudoaromatic heterocycles which are heterocyclic substituents that have similar properties and structures (nearly planar) to aromatic heterocyclic ligands, but are not by definition aromatic; likewise the term aromatic also refers to substituted aromatics.

The term “arylalkyl” means an aryl group where a hydrogen has been replaced with an alkyl or substituted alkyl group. For example, 3,5′-di-tert-butyl-phenyl indenyl is an indene substituted with an arylalkyl group. When an arylalkyl group is a substituent on another group, it is bound to that group via the aryl. For example in Formula (AI), the aryl portion is bound to E.

The term “alkylaryl” means an alkyl group where a hydrogen has been replaced with an aryl or substituted aryl group. For example, phenethyl indenyl is an indene substituted with an ethyl group bound to a benzene group. When an alkylaryl group is a substituent on another group, it is bound to that group via the alkyl. For example in Formula (AI), the alkyl portion is bound to E.

Where isomers of a named alkyl, alkenyl, alkoxide, or aryl group exist (e.g., n-butyl, iso-butyl, sec-butyl, and tert-butyl) reference to one member of the group (e.g., n-butyl) shall expressly disclose the remaining isomers (e.g., iso-butyl, sec-butyl, and tert-butyl) in the family. Likewise, reference to an alkyl, alkenyl, alkoxide, or aryl group without specifying a particular isomer (e.g., butyl) expressly discloses all isomers (e.g., n-butyl, iso-butyl, sec-butyl, and tert-butyl).

The term “ring atom” means an atom that is part of a cyclic ring structure. By this definition, a benzyl group has six ring atoms and tetrahydrofuran has 5 ring atoms.

A heterocyclic ring is a ring having a heteroatom in the ring structure as opposed to a heteroatom substituted ring where a hydrogen on a ring atom is replaced with a heteroatom. For example, tetrahydrofuran is a heterocyclic ring and 4-N,N-dimethylamino-phenyl is a heteroatom-substituted ring. Other examples of heterocycles may include pyridine, imidazole, and thiazole.

The term “azole” means a five-membered heterocyclic compound containing a nitrogen, at least one other non-carbon atom (e.g., nitrogen, sulfur, or oxygen) as part of the heterocyclic ring, and two double-bonds. An azole is an aromatic compound. Examples of azoles may include pyrazole, imidazole, thiazole, oxazole, isoxazole, and azaphosphole.

The terms “hydrocarbyl radical,” “hydrocarbyl group,” or “hydrocarbyl” may be used interchangeably and are defined to mean a group consisting of hydrogen and carbon atoms only. For example, a hydrocarbyl can be a C₁-C₁₀₀ radical that may be linear, branched, or cyclic, and when cyclic, aromatic or non-aromatic. Examples of such radicals may include, but are not limited to, alkyl groups such as methyl, ethyl, propyl (such as n-propyl, isopropyl, cyclopropyl), butyl (such as n-butyl, isobutyl, sec-butyl, tert-butyl, cyclobutyl), pentyl (such as iso-amyl, cyclopentyl) hexyl (such as cyclohexyl), octyl (such as cyclooctyl), nonyl, decyl (such as adamantyl), undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl, octadecyl, nonadecyl, icosyl, henicosyl, docosyl, tricosyl, tetracosyl, pentacosyl, hexacosyl, heptacosyl, octacosyl, nonacosyl, or tricontyl, and aryl groups, such as phenyl, benzyl, and naphthyl.

Unless otherwise indicated, as used herein, “low comonomer content” is defined as a polyolefin having less than 8 wt % of comonomer based upon the total weight of the polyolefin. As used herein, “high comonomer content” is defined as a polyolefin having greater than or equal to 8 wt % of comonomer based upon the total weight of the polyolefin.

As used herein, Mn is number average molecular weight, Mw is weight average molecular weight, and Mz is z average molecular weight, wt % is weight percent, and mol % is mole percent. Molecular weight distribution (MWD), also referred to as polydispersity index (PDI), is defined to be Mw divided by Mn. Unless otherwise noted, all molecular weight units (e.g., Mw, Mn, Mz) are g/mol.

Unless otherwise indicated, as used herein, “high molecular weight” is defined as a weight average molecular weight (Mw) value of 100,000 g/mol or more. “Low molecular weight” is defined as an Mw value of less than 100,000 g/mol, such as 10,500 g/mol or less. “Very low molecular weight” is defined as an Mw value of 6,000 g/mol or less.

Unless otherwise noted all melting points (Tm) are differential scanning calorimetry (DSC) second melt.

A “catalyst system” is a combination of at least one catalyst compound, at least one activator, an optional coactivator, and an optional support material. The terms “catalyst compound”, “catalyst complex”, “transition metal complex”, “transition metal compound”, “precatalyst compound”, and “precatalyst complex” are used interchangeably. When “catalyst system” is used to describe such a pair before activation, it means the unactivated catalyst complex (precatalyst) together with an activator and, optionally, a coactivator. When it is used to describe such a pair after activation, it means the activated complex and the activator or other charge-balancing moiety. The transition metal compound may be neutral as in a precatalyst, or a charged species with a counter ion as in an activated catalyst system. For the purposes of the present disclosure and the claims thereto, when catalyst systems are described as comprising neutral stable forms of the components, it is well understood by one of ordinary skill in the art, that the ionic form of the component is the form that reacts with the monomers to produce polymers. A polymerization catalyst system is a catalyst system that can polymerize monomers to polymer. Furthermore, catalyst compounds and activators represented by formulae herein embrace both neutral and ionic forms of the catalyst compounds and activators.

In the description herein, the catalyst may be described as a catalyst, a catalyst precursor, a pre-catalyst compound, catalyst compound or a transition metal compound, and these terms are used interchangeably.

An “anionic ligand” is a negatively charged ligand which donates one or more pairs of electrons to a metal ion. A “Lewis base” is a neutrally charged ligand which donates one or more pairs of electrons to a metal ion. Examples of Lewis bases include ethylether, trimethylamine, pyridine, tetrahydrofuran, dimethylsulfide, and triphenylphosphine. The term “heterocyclic Lewis base” refers to Lewis bases that are also heterocycles. Examples of heterocyclic Lewis bases include pyridine, imidazole, thiazole, 1,3-azaphosphole, and furan. The bis(aryl phenolate) Lewis base ligands are tridentate ligands that bind to the metal via two anionic donors (e.g., phenolates) and one heterocyclic Lewis base donor that is a heterocyclic ring having 5 ring atoms (e.g., a thiazolyl group).

A scavenger is a compound that can be added to facilitate polymerization by scavenging impurities. Some scavengers may also act as activators and may be referred to as coactivators. A coactivator, that is not a scavenger, may also be used in conjunction with an activator in order to form an active catalyst. In at least one embodiment, a coactivator can be pre-mixed with the transition metal compound to form an alkylated transition metal compound.

Noncoordinating anion (NCA) is defined to mean an anion either that does not coordinate to the catalyst metal cation or that does coordinate to the metal cation, but only weakly. The term NCA is also defined to include multicomponent NCA-containing activators, such as N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, that contain an acidic cationic group and the non-coordinating anion. The term NCA is also defined to include neutral Lewis acids, such as tris(pentafluorophenyl)boron, that can react with a catalyst to form an activated species by abstraction of an anionic group. A Lewis acid is defined to be a compound or element that can react with an electron donor to form a bond. An NCA coordinates weakly enough that a Lewis base, such as an olefin monomer can displace it from the catalyst center. Any metal or metalloid that can form a compatible, weakly coordinating complex may be used or contained in the non-coordinating anion. Suitable metals include, but are not limited to, aluminum, gold, and platinum. Suitable metalloids include, but are not limited to, boron, aluminum, phosphorus, and silicon.

The term “continuous” means a system that operates without interruption or cessation. For example a continuous process to produce a polymer would be one where the reactants are continually introduced into one or more reactors and polymer product is continually withdrawn.

A solution polymerization means a polymerization process in which the polymer is dissolved in a liquid polymerization medium, such as an inert solvent or monomer(s) or their blends. A solution polymerization can be homogeneous. A homogeneous polymerization is one where the polymer product is dissolved in the polymerization medium. Suitable systems may be not turbid as described in J. Vladimir Oliveira, C. Dariva and J. C. Pinto, Ind. Eng. Chem. Res., 2000, v. 29, p. 4627.

A bulk polymerization means a polymerization process in which the monomers and/or comonomers being polymerized are used as a solvent or diluent using little or no inert solvent as a solvent or diluent. A small fraction of inert solvent might be used as a carrier for catalyst and scavenger. A bulk polymerization system contains less than 25 wt % of inert solvent or diluent, such as less than 10 wt %, such as less than 1 wt %, such as 0 wt %.

Transition Metal Complexes

In at least one embodiment, the present disclosure relates to catalyst compounds having a Lewis base tridentate ligand, such as a bis(aryl phenolate) five-membered heterocyclic ring-tridentate ligand, which coordinates to a group 3, 4, or 5 transition metal center, forming two eight-membered rings.

A catalyst compound can be represented by Formula (I):

wherein:

M is a group 3, 4, or 5 metal;

each A¹, A², A³, and A⁴ is independently an aromatic group;

J is a heterocyclic Lewis base;

each Q¹ and Q² are independently selected from O, S, N(R³⁰), or P(R³⁰), wherein R³⁰ is C₁-C₄₀ hydrocarbyl, substituted C₁-C₄₀ hydrocarbyl, or a heteroatom, or a heteroatom-containing group;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand,

wherein the ring formed by M, Q¹, A³, A¹, and J is an eight-membered ring and the ring formed by M, Q², A⁴, A² and, J is an eight-membered ring.

In at least one embodiment, the catalyst compound represented by Formula (I) is represented by Formula (II):

wherein:

M is a group 3, 4, or 5 metal;

A¹ and A² are independently an aromatic group;

J is a heterocyclic Lewis base;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, or a heteroatom, or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms, and where substitutions on the ring can join to form additional rings;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand,

wherein the ring formed by M, O, A¹, and J is an eight-membered ring and the ring formed by M, O, A², and J is an eight-membered ring.

In at least one embodiment, J is a heterocyclic ring having 5 ring atoms. In at least one embodiment, J is a heterocyclic ring having 6 ring atoms. In alternate embodiments of the invention, J preferably contains 1, 2 or more ring atoms that are heteroatoms. Preferably, when J is a six membered ring, the ring contains at least 2 ring heteroatoms (which may be the same or different), preferably J contains at least two of S, N, P, or O as ring atoms (which may be the same or different). Alternately, when J is a five membered ring, the ring contains at least 1 heteroatom ring atom, preferably J contains at least one of S, N, P, O as a ring atom. Alternately J may be a five membered ring, and the ring contains at least 2 heteroatom ring atoms (which may be the same or different), preferably J contains at least two of S, N, P, or O as ring atoms (which may be the same or different).

In at least one embodiment, A¹ is represented by the formula:

where

indicates a connection to the catalyst compound, and each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.

In at least one embodiment, A² is represented by the formula:

where

indicates a connection to the catalyst compound, and each of R¹³, R¹, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.

In at least one embodiment, J is represented by the formula:

where

indicates a connection to the catalyst compound, and R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group. E can be an unsubstituted heteroatom or a substituted heteroatom. For example, E can be S, carbon (such that J is a pyrrole), nitrogen (such that J is an imidazole), oxygen (such that J is an oxazole), or phosphorus (such that J is an azaphosphole).

In at least one embodiment, J is represented by the formula:

such as

where

indicates a connection to the catalyst compound, and each Z is independently an unsubstituted heteroatom or a substituted heteroatom. For example, Z can be sulfur, carbon, nitrogen, oxygen, or phosphorus.

In at least one embodiment, the catalyst compound represented by Formula (II) is represented by Formula (III):

wherein:

M is a group 3, 4, or 5 metal;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2, or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

E is an unsubstituted heteroatom or substituted heteroatom (such as S, O, N(R¹⁸) or P(R¹⁸) where R¹⁸ is hydrogen or C₁-C₁₀ hydrocarbyl, C₁-C₁₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group);

each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms;

each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms;

each of R¹³, R¹⁴, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms;

R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand group.

For example, M of Formula (I), Formula (II), or Formula (III) can be a group 3, 4 or 5 metal, such as M can be a group 4 metal. Group 4 metals may include zirconium, titanium, and hafnium. In at least one embodiment, M is zirconium or hafnium.

Each L of Formula (I), Formula (II), or Formula (III) can be independently selected from ethers, amines, phosphines, thioethers, esters, Et₂O, MeOtBu, Et₃N, PhNMe₂, MePh₂N, tetrahydrofuran, and dimethylsulfide, and each X can be independently selected from methyl, benzyl, trimethylsilyl, neopentyl, ethyl, propyl, butyl, phenyl, hydrido, chloro, fluoro, bromo, iodo, trifluoromethanesulfonate, dimethylamido, diethylamido, dipropylamido, and diisopropylamido. In at least one embodiment, n of Formula (I), Formula (II), or Formula (III) is 2 and each X is independently chloro or methyl.

The Lewis base (J) of Formula (I), or Formula (II) can be selected from cyclic Lewis bases. The Lewis base J is a divalent group that bridges the A¹ and A² groups and is coordinated to the metal center M as a neutral 2-electron donor. The Lewis base J may be an aromatic or non-aromatic heterocyclic. The Lewis base J may be a heterocyclic Lewis base having 5 or 6 ring atoms. In at least one embodiment, J is a group 15-containing heterocycle, or a group 16-containing heterocycle, such as J is a nitrogen-containing heterocycle, an oxygen-containing heterocycle, a phosphorus-containing heterocycle, or a sulfur-containing heterocycle, for example. 5-membered heterocyclic Lewis bases may include thiazoles, isothiazoles, 1,2,4-thidiazoles, 1,2,5-thidiazoles, 1,3,4-thidiazoles, thiophenes, oxazoles, isoxazoles, oxazolines (e.g., 2-oxazoline, 3-oxazoline, 4-oxazoline), oxazolidines, imidazoles, furans, thiofurans, pyrroles, pyrazoles, 1,2,3-triazoles, 1,2,4-triazoles, boroles, phospholes, azaphospholes, or isomers thereof, substituted or unsubstituted.

R¹⁷ of Formula (III) can be hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group. In at least one embodiment, R¹⁷ is hydrogen.

E of Formula (III) can be selected from group 15 or 16 atoms (e.g., sulfur (such as J=thiazole); oxygen (such as J=oxazole)), nitrogen (e.g., N(R¹⁸) where R¹⁸ is hydrogen or C₁-C₁₀ hydrocarbyl, C₁-C₁₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group), or phosphorus (e.g., P(R¹⁹) where R¹⁹ is hydrogen or C₁-C₁₀ hydrocarbyl, C₁-C₁₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group). In at least one embodiment, E is sulfur.

Each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ of Formula (II) or Formula (III) can be independently selected from hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, alkoxy, silyl, amino, aryloxy, halogen, or phosphino, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.

In at least one embodiment, one or more of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, R⁸ of Formula (II) (where applicable) or Formula (III) is independently selected from methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, phenyl, substituted phenyl, biphenyl or an isomer thereof, which may be halogenated (such as perfluoropropyl, perfluorobutyl, perfluoroethyl, perfluoromethyl), substituted hydrocarbyl radicals and all isomers of substituted hydrocarbyl radicals including trimethylsilylpropyl, trimethylsilylmethyl, trimethyl silylethyl, phenyl, or all isomers of hydrocarbyl substituted phenyl including methylphenyl, dimethylphenyl, trimethylphenyl, tetramethylphenyl, pentamethylphenyl, diethylphenyl, triethylphenyl, propylphenyl, dipropylphenyl, tripropylphenyl, dimethylethylphenyl, dimethylpropylphenyl, dimethylbutylphenyl, or dipropylmethylphenyl.

For example, R⁴ and R⁵ of Formula (II) (where applicable) or Formula (III) can be independently C₁-C₁₀ alkyl, such as R⁴ and R⁵ can be tert-butyl. In at least one embodiment, R⁴ and R⁵ are independently selected from unsubstituted phenyl, substituted phenyl, unsubstituted carbazole, substituted carbazole, unsubstituted naphthyl, substituted naphthyl, unsubstituted anthracenyl, substituted anthracenyl, unsubstituted fluorenyl, or substituted fluorenyl, a heteroatom or a heteroatom-containing group, such as R⁴ and R⁵ can be independently unsubstituted phenyl or 3,5-di-tert-butylbenzyl. Furthermore, either (1) R⁴ can be C₁-C₁₀ alkyl (e.g., R⁴ can be tert-butyl) and R⁵ can be an aryl, or (2) R⁵ can be C₁-C₁₀ alkyl (e.g., R⁵ can be tert-butyl) and R⁴ can be an aryl. Alternately, R⁴ and/or R⁵ can be independently a heteroatom, such as R⁴ and R⁵ can be a halogen atom (such as Br, Cl, F, or I).

In at least one embodiment, each R² and R⁷ of Formula (II) (where applicable) or Formula (III) is independently C₁-C₁₀ alkyl, such as R² and R⁷ are independently methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, dimethyl-pentyl, tert-butyl, isopropyl, or isomers thereof.

Each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ of Formula (II) (or Formula (I) where applicable) can be independently hydrogen or C₁-C₁₀ alkyl, such as R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ can be independently hydrogen, methyl, ethyl, propyl, or isopropyl. In at least one embodiment, R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ are hydrogen. Alternately, each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ of Formula (III) (or Formula (II) where applicable) can be independently hydrogen, phenyl, cyclohexyl, fluoro, chloro, methoxy, ethoxy, phenoxy, or trimethylsilyl.

In at least one embodiment, the catalyst compound of Formula (II) is one or more of:

In at least one embodiment, the catalyst compound represented by Formula (II) is selected from:

In at least one embodiment, the catalyst compound represented by Formula (II) is selected from:

In at least one embodiment, one or more different catalyst compounds are present in a catalyst system. One or more different catalyst compounds can be present in the reaction zone where the process(es) described herein occur. The same activator can be used for the transition metal compounds, however, two different activators, such as a non-coordinating anion activator and an alumoxane, can be used in combination.

The two transition metal compounds (pre-catalysts) may be used in any ratio. Molar ratios of (A) transition metal compound to (B) transition metal compound can be a range of (A:B) of from 1:1000 to 1000:1, alternatively 1:100 to 500:1, alternatively 1:10 to 200:1, alternatively 1:1 to 100:1, alternatively 1:1 to 75:1, and alternatively 5:1 to 50:1. The particular ratio chosen will depend on the exact pre-catalysts chosen, the method of activation, and the end product desired. In at least one embodiment, when using the two pre-catalysts, where both are activated with the same activator, mole percentages, based upon the molecular weight of the pre-catalysts, can be from 10% to 99.9% A to 0.1% to 90% B, alternatively 25% to 99% A to 0.5% to 75% B, alternatively 50% to 99% A to 1% to 50% B, and alternatively 75% to 99% A to 1% to 10% B.

Methods to Prepare the Catalyst Compounds

The following describes methods to prepare catalysts described herein. FIG. 2 illustrates the bis(arylphenolate)heterocycle complexes, the free ligand, and the key fragments of the free ligand. Catalyst compounds of this type can be synthesized as described below (and in the Examples), where free ligand can be obtained via a multiple reaction process in order to join together the three fragments (i.e., heterocyclic group, aryl linker group, and the phenolate group). The joining of the aryl linker with the phenolate group to produce an aryl phenol fragment can be accomplished via reaction of an ortho-metalated protected phenol with a 1,2-dihalobenzene. For example, a protected 2-bromophenol can be converted to a Grignard reagent by reaction with a magnesium metal. The Grignard reagent may then be reacted with 1-bromo-2-chlorobenzene to form the protected aryl-phenol product. When the reaction is performed in the presence of excess magnesium, the reaction can be then followed by a quenching reaction of the resulting product with 2-isopropoxy-4,4,5,5-tetramethyl-1,3,2-dioxaborolane, which can lead to the formation of the boronic acid ester form of the protected aryl phenol. The boronic acid ester can then be coupled to the heterocyclic group in a palladium-catalyzed Suzuki reaction between the boronic acid ester and a dihalogenated heterocycle, such as 2,4-dibromothiazole, for example. Other dihalogenated heterocycles can be used. While the aforementioned route uses a boronic acid ester in a Suzuki-type coupling reaction, any other suitable coupling reaction can be used to target the same product. For example, the protected aryl phenol Grignard reagent could be reacted with zinc chloride to form an organozinc reagent that could be used in a Negishi type coupling reaction with a dihalogenated heterocycle. Similarly, the Grignard reagent could be used in a Kumada coupling reaction with a dihalogenated heterocycle. Once the free ligand has been prepared, the free ligand can be converted to the corresponding transition metal complex by reaction with metal-containing reagents. Examples of suitable metal-containing reagents may include metal halides, metal amides, and organometallics. For example, metal-containing reagents may include ZrCl₄, HfCl₄, Zr(NMe₂)₄, Hf(NEt₂)₄, Zr(CH₂Ph)₄, Hf(CH₂Ph)₄, or TiCl₄. The free ligand may be: i) reacted directly with the metal-containing reagents; or ii) deprotonated by reaction with a main-group metal reagent (e.g., BuLi, NaH, iPrMgBr, MeMgBr) prior to reaction with the transition metal reagent. Alternatively, the metal halide reagents may be reacted with an alkylating agent, such as an organomagnesium reagent, to form in situ a transition metal organometallic species that can be subsequently reacted with the free ligand to form the catalyst complex.

Activators

The terms “cocatalyst” and “activator” are used herein interchangeably.

The catalyst systems described herein may comprise a catalyst complex as described above and an activator such as alumoxane or a non-coordinating anion and may be formed by combining the catalyst components described herein with activators in any manner known from the literature including combining them with supports, such as silica. The catalyst systems may also be added to or generated in solution polymerization or bulk polymerization (in the monomer). Catalyst systems of the present disclosure may have one or more activators and one, two or more catalyst components. Activators are defined to be any compound which can activate any one of the catalyst compounds described above by converting the neutral metal compound to a catalytically active metal compound cation. Non-limiting activators, for example, may include alumoxanes, aluminum alkyls, ionizing activators, which may be neutral or ionic, and conventional-type cocatalysts. Suitable activators may include alumoxane compounds, modified alumoxane compounds, and ionizing anion precursor compounds that abstract a reactive, G-bound, metal ligand making the metal compound cationic and providing a charge-balancing non-coordinating or weakly coordinating anion, e.g., a non-coordinating anion.

In at least one embodiment, the catalyst system includes an activator and the catalyst compound of Formula (I), Formula (II), or Formula (III). The identity of the activator combined with the identity of the catalyst compound of Formula (I), Formula (II), or Formula (III) can be used to control the activity of the catalyst. For example, in the case of a polymerization or copolymerization of an olefin such as ethylene, when a catalyst compound of Formula (I), Formula (II), or Formula (III) is combined with an ionizing/non-coordinating anion activators (e.g., N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate), the catalyst activity of the catalyst compound of Formula (I), Formula (II), or Formula (III) may be ≥30,000 gP·mmolcat⁻¹·h⁻¹, such as 35,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 40,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 50,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 75,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 100,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 150,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 200,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 250,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 300,000 gP·mmolcat⁻¹·h⁻¹ or greater, such as 400,000 gP·mmolcat⁻¹·h⁻¹ or greater (e.g., about 379,906 gP·mmolcat⁻¹·h⁻¹). In contrast, when a catalyst compound of Formula (I), Formula (II), or Formula (III) is combined with an alumoxane activator (e.g., MAO), the catalyst activity of the catalyst compound of Formula (I), Formula (II), or Formula (III) can be ≤30,000 gP·mmolcat⁻¹·h⁻¹, such as from about 50 gP·mmolcat⁻¹·h⁻¹ to about 30,000 gP·mmolcat⁻¹·h⁻¹, such as from about 100 gP·mmolcat⁻¹·h⁻¹ to about 25,000 gP·mmolcat⁻¹·h⁻¹. Furthermore, the identity of the activator combined with the identity of the catalyst compound of Formula (I), Formula (II), or Formula (III) can be used to control the molecular weight of the polymer products, and the Tm of the polymer products. For example, when an ionizing/non-coordinating anion activator (e.g., N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate) is combined with the catalyst compound of Formula (I), Formula (II), or Formula (III), low or very low molecular weight polymers (e.g., <100,000 g/mol, such as from about 1,000 g/mol to about 20,000 g/mol, such as from about 2,000 g/mol to about 15,000 g/mol) can be formed and may have Tm values lower than that of the polymers formed using an alumoxane activator (e.g., MAO). In contrast, when an alumoxane activator (e.g., MAO), is combined with the catalyst compound of Formula (I), Formula (II), or Formula (III), high molecular weight polymers (e.g., ≥100,000 g/mol, such as from about 100,000 g/mol to about 3,000,000 g/mol, such as from about 500,000 g/mol to about 2,000,000 g/mol) can be formed and may have Tm values higher than that of the polymers formed using an ionizing/non-coordinating anion activators.

Alumoxane Activators

Alumoxane activators are utilized as activators in the catalyst systems described herein. Alumoxanes are generally oligomeric compounds containing —Al(R^(a′″))—O— sub-units, where R^(a′″) is an alkyl group. Examples of alumoxanes include methylalumoxane (MAO), modified methylalumoxane (MMAO), ethylalumoxane and isobutylalumoxane. Alkylalumoxanes and modified alkylalumoxanes are suitable as catalyst activators, particularly when the abstractable ligand is an alkyl, halide, alkoxide or amide. Mixtures of different alumoxanes and modified alumoxanes may also be used. It may be suitable to use a visually clear methylalumoxane. A cloudy or gelled alumoxane can be filtered to produce a clear solution or clear alumoxane can be decanted from the cloudy solution. A useful alumoxane is a modified methyl alumoxane (MMAO) cocatalyst type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylalumoxane type 3A, covered under patent number U.S. Pat. No. 5,041,584, which is incorporated by reference herein). Another useful alumoxane is solid polymethylaluminoxane as described in U.S. Pat. Nos. 9,340,630, 8,404,880, and 8,975,209, which are incorporated by reference herein.

When the activator is an alumoxane (modified or unmodified), at least one embodiment select the maximum amount of activator at up to a 5,000-fold molar excess Al/M over the catalyst compound (per metal catalytic site). The minimum activator-to-catalyst-compound can be a 1:1 molar ratio. Alternate ranges may include from 1:1 to 500:1, alternately from 1:1 to 200:1, alternately from 1:1 to 100:1, or alternately from 1:1 to 50:1.

In an alternate embodiment, little or no alumoxane is used in the polymerization processes described herein. For example, alumoxane can be present at zero mole %, alternately the alumoxane can be present at a molar ratio of aluminum to catalyst compound transition metal less than 500:1, such as less than 300:1, such as less than 100:1, such as less than 1:1.

Ionizing/Non-Coordinating Anion Activators

The term “non-coordinating anion” (NCA) means an anion which either does not coordinate to a cation or which is only weakly coordinated to a cation thereby remaining sufficiently labile to be displaced by a Lewis base. “Compatible” non-coordinating anions are those which are not degraded to neutrality when the initially formed complex decomposes. Further, the anion will not transfer an anionic substituent or fragment to the cation so as to cause it to form a neutral transition metal compound and a neutral by-product from the anion. Non-coordinating anions useful in accordance with the present disclosure are those that are compatible, stabilize the transition metal cation in the sense of balancing its ionic charge at +1, and yet retain sufficient lability to permit displacement during polymerization. Ionizing activators useful herein typically comprise an NCA, particularly a compatible NCA.

It is within the scope of the present disclosure to use an ionizing activator, neutral or ionic. It is also within the scope of the present disclosure to use neutral or ionic activators alone or in combination with alumoxane or modified alumoxane activators. For descriptions of suitable activators please see U.S. Pat. Nos. 8,658,556 and 6,211,105.

The catalyst systems of the present disclosure can include at least one non-coordinating anion (NCA) activator. In at least one embodiment, boron containing NCA activators represented by the formula below can be used:

Z_(d) ⁺(A^(d-))

where: Z is (L-H) or a reducible Lewis acid; L is a Lewis base; H is hydrogen;

(L-H) is a Bronsted acid; A^(d-) is a boron containing non-coordinating anion having the charge d−; d is 1, 2, or 3.

The cation component, Z_(d) ⁺ may include Bronsted acids such as protons or protonated Lewis bases or reducible Lewis acids capable of protonating or abstracting a moiety, such as an alkyl or aryl, from the bulky ligand transition metal catalyst precursor, resulting in a cationic transition metal species.

The activating cation Z_(d) ⁺ may also be a moiety such as silver, tropylium, carbeniums, ferroceniums and mixtures, such as carbeniums and ferroceniums. Z_(d) ⁺ can be triphenyl carbenium. Reducible Lewis acids can be a triaryl carbenium (where the aryl can be substituted or unsubstituted, such as those represented by the formula: (Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl, or a substituted C₁ to C₄₀ hydrocarbyl), such as the reducible Lewis acids “Z” may include those represented by the formula: (Ph₃C), where Ph is a substituted or unsubstituted phenyl, such as substituted with C₁ to C₄₀ hydrocarbyls or substituted a C₁ to C₄₀ hydrocarbyls, such as C₁ to C₂₀ alkyls or aromatics or substituted C₁ to C₂₀ alkyls or aromatics, such as Z is a triphenylcarbenium.

When Z_(d) ⁺ is the activating cation (L-H)_(d) ⁺, it can be a Bronsted acid, capable of donating a proton to the transition metal catalytic precursor resulting in a transition metal cation, including ammoniums, oxoniums, phosphoniums, silyliums, and mixtures thereof, such as ammoniums of methylamine, aniline, dimethylamine, diethylamine, N-methylaniline, diphenylamine, trimethylamine, triethylamine, N,N-dimethylaniline, methyldiphenylamine, pyridine, p-bromo N,N-dimethylaniline, p-nitro-N,N-dimethylaniline, dioctadecylmethylamine, phosphoniums from triethylphosphine, triphenylphosphine, and diphenylphosphine, oxoniums from ethers such as dimethyl ether diethyl ether, tetrahydrofuran and dioxane, sulfoniums from thioethers, such as diethyl thioethers, tetrahydrothiophene, and mixtures thereof.

The anion component A^(d-) includes those having the formula [M^(k+)Q_(n)]^(d-) where k is 1, 2, or 3; n is 1, 2, 3, 4, 5, or 6 (such as 1, 2, 3, or 4); n−k=d; M is an element selected from Group 13 of the Periodic Table of the Elements, such as boron or aluminum, and Q is independently a hydride, bridged or unbridged dialkylamido, halide, alkoxide, aryloxide, hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, and halosubstituted-hydrocarbyl radicals, said Q having up to 20 carbon atoms with the proviso that in not more than 1 occurrence is Q a halide. Each Q can be a fluorinated hydrocarbyl group having 1 to 20 carbon atoms, such as each Q is a fluorinated aryl group, and such as each Q is a pentafluoryl aryl group. Examples of suitable A^(d-) also include diboron compounds as disclosed in U.S. Pat. No. 5,447,895, which is fully incorporated herein by reference.

Illustrative, but not limiting, examples of boron compounds which may be used as an activating cocatalyst are the compounds described as (and particularly those specifically listed as) activators in U.S. Pat. No. 8,658,556, which is incorporated by reference herein.

The ionic activator Z_(d) ⁺ (A^(d-)) can be one or more of N,N-dimethylanilinium tetrakis(perfluorophenyl)borate, N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate, dioctadecylmethylammonium tetrakis(perfluorophenyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, or triphenylcarbenium tetra(perfluorophenyl)borate.

Alternately, the activator compounds are represented by Formula (AI):

[R¹R²R³EH]_(d) ⁺[M^(k+)Q_(n)]^(d-)  (AI)

wherein:

E is nitrogen or phosphorous, preferably nitrogen;

d is 1, 2 or 3 (preferably 3); k is 1, 2, or 3 (preferably 3); n is 1, 2, 3, 4, 5, or 6 (preferably 4, 5, or 6); n−k=d (preferably d is 1, 2 or 3; k is 3; n is 4, 5, or 6, preferably when M is B, n is 4);

each of R¹, R², and R³ is independently H, optionally substituted C₁-C₄₀ alkyl (such as branched or linear alkyl), or optionally substituted C₅-C₅₀-aryl (alternately each of R¹, R², and R³ is independently unsubstituted or substituted with at least one of halide, C₅-C₅₀ aryl, C₆-C₃₅ arylalkyl, C₆-C₃₅ alkylaryl and, in the case of the C₅-C₅₀-aryl, C₁-C₅₀ alkyl); wherein R¹, R², and R³ together comprise 15 or more carbon atoms (such as 18 or more carbon atoms, such as 20 or more carbon atoms, such as 22 or more carbon atoms, such as 25 or more carbon atoms, such as 30 or more carbon atoms, such as 35 or more carbon atoms, such as 37 or more carbon atoms, such as 40 or more carbon atoms, such as 45 or more carbon atoms), preferably at least one of R¹, R², and R³ is a C₃ to C₄₀ hydrocarbyl, (such as a C₃-C₄₀ alkyl, alternately such as a C₇ to C₄₀ alkyl);

M is an element selected from group 13 of the Periodic Table of the Elements, preferably B or Al, preferably B; and

each Q is independently a hydride, bridged or unbridged dialkylamido, halide, alkoxide, aryloxide, hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, or halosubstituted-hydrocarbyl radical, preferably a fluorinated aryl group, such fluoro-phenyl or fluoro-naphthyl, more preferably perfluorophenyl or perfluoronaphthyl.

In any embodiment of Formula (AI), each of R¹, R² and R³ may independently be selected from:

1) optionally substituted linear alkyls (such as methyl, ethyl, n-propyl, n-butyl, n-pentyl, n-hexyl, n-heptyl, n-octyl, n-nonyl, n-decyl, n-undecyl, n-dodecyl, n-tridecyl, n-tetradecyl, n-pentadecyl, n-hexadecyl, n-heptadecyl, n-octadecyl, n-nonadecyl, n-icosyl, n-henicosyl, n-docosyl, n-tricosyl, n-tetracosyl, n-pentacosyl, n-hexacosyl, n-heptacosyl, n-octacosyl, n-nonacosyl, or n-tricontyl);

2) optionally substituted branched alkyls (such as alkyl-butyl, alkyl-pentyl, alkyl-hexyl, alkyl-heptyl, alkyl-octyl, alkyl-nonyl, alkyl-decyl, alkyl-undecyl, alkyl-dodecyl, alkyl-tridecyl, alkyl-butadecyl, alkyl-pentadecyl, alkyl-hexadecyl, alkyl-heptadecyl, alkyl-octadecyl, alkyl-nonadecyl, alkyl-icosyl (including multi-alkyl analogs, i.e, dialkyl-butyl, dialkyl-pentyl, dialkyl-hexyl, dialkyl-heptyl, dialkyl-octyl, dialkyl-nonyl, dialkyl-decyl, dialkyl-undecyl, dialkyl-dodecyl, dialkyl-tridecyl, dialkyl-butadecyl, dialkyl-pentadecyl, dialkyl-hexadecyl, dialkyl-heptadecyl, dialkyl-octadecyl, dialkyl-nonadecyl, dialkyl-icosyl, trialkyl-butyl, trialkyl-pentyl, trialkyl-hexyl, trialkyl-heptyl, trialkyl-octyl, trialkyl-nonyl, trialkyl-decyl, trialkyl-undecyl, trialkyl-dodecyl, trialkyl-tridecyl, trialkyl-butadecyl, trialkyl-pentadecyl, trialkyl-hexadecyl, trialkyl-heptadecyl, trialkyl-octadecyl, trialkyl-nonadecyl, and trialkyl-icosyl, etc.), and isomers thereof wherein each alkyl group is independently a C₁ to C₄₀, (alternately C₂ to C₃₀, alternately C₃ to C₂₀) linear, branched or cyclic alkyl group), preferably the alkyl group is methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl, octadecyl, nonadecyl, icosyl, henicosyl, docosyl, tricosyl, tetracosyl, pentacosyl, hexacosyl, heptacosyl, octacosyl, nonacosyl, or tricontyl);

3) optionally substituted arylalkyls, such as (methylphenyl, ethylphenyl, propylphenyl, butylphenyl, pentylphenyl, hexylphenyl, heptylphenyl, octylphenyl, nonylphenyl, decylphenyl, undecylphenyl, dodecylphenyl, tridecylphenyl, tetradecylphenyl, pentadecylphenyl, hexadecylphenyl, heptadecylphenyl, octadecylphenyl, nonadecylphenyl, icosylphenyl, henicosylphenyl, docosylphenyl, tricosylphenyl, tetracosylphenyl, pentacosylphenyl, hexacosylphenyl, heptacosylphenyl, octacosylphenyl, nonacosylphenyl, tricontylphenyl, 3,5,5-trimethylhexylphenyl, dioctylphenyl, 3,3,5-trimethylhexylphenyl, 2,2,3,3,4 pentamethypentylylphenyl, and the like);

4) optionally substituted silyl groups, such as a trialkylsilyl group, where each alkyl is independently an optionally substituted C₁ to C₂₀ alkyl (such as trimethylsilyl, triethylsilyl, tripropylsilyl, tributylsilyl, trihexylsilyl, triheptylsilyl, trioctylsilyl, trinonylsilyl, tridecylsilyl, triundecylsilyl, tridodecylsilyl, tri-tridecylsilyl, tri-tetradecylsilyl, tri-pentadecylsilyl, tri-hexadecylsilyl, tri-heptadecylsilyl, tri-octadecylsilyl, tri-nonadecylsilyl, tri-icosylsilyl);

5) optionally substituted alkoxy groups (such as —OR*, where R* is an optionally substituted C₁ to C₂₀ alkyl or aryl (such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl, heptadecyl, octadecyl, nonadecyl, icosyl, phenyl, alkylphenyl (such as methyl phenyl, propyl phenyl, etc.), naphthyl, or anthracenyl);

6) halogens (such as Br or Cl); and

7) halogen containing groups (such as bromomethyl, bromophenyl, and the like).

For more information on activators represented by Formula (IA) that are useful herein please see US2019-0330139 and US2019-0330392, which are incorporated by reference herein. Useful activators include N-methyl-4-nonadecyl-N-octadecylanilinium tetrakis(perfluoronaphthalen-2-yl)borate, and N-methyl-4-nonadecyl-N-octadecylanilinium tetrakis(perfluorophenyl)borate.

Bulky activators are also useful herein as NCAs. “Bulky activator” as used herein refers to anionic activators represented by the formula:

where:

each R^(A) is independently a halide, such as a fluoride;

Ar is substituted or unsubstituted aryl group (such as a substituted or unsubstituted phenyl), such as substituted with C₁ to C₄₀ hydrocarbyls, such as C₁ to C₂₀ alkyls or aromatics;

each R^(B) is independently a halide, a C₆ to C₂₀ substituted aromatic hydrocarbyl group or a siloxy group of the formula —O—Si—R^(D), where R^(D) is a C₁ to C₂₀ hydrocarbyl or hydrocarbylsilyl group (such as R^(B) is a fluoride or a perfluorinated phenyl group);

each R^(C) is a halide, C₆ to C₂₀ substituted aromatic hydrocarbyl group or a siloxy group of the formula —O—Si—R^(D), where R^(D) is a C₁ to C₂₀ hydrocarbyl or hydrocarbylsilyl group (such as R^(D) is a fluoride or a C₆ perfluorinated aromatic hydrocarbyl group); where R^(B) and R^(C) can form one or more saturated or unsaturated, substituted or unsubstituted rings (such as R^(B) and R^(C) form a perfluorinated phenyl ring);

L is a Lewis base; (L-H)⁺ is a Bronsted acid; d is 1, 2, or 3;

where the anion has a molecular weight of greater than 1,020 g/mol; and

where at least three of the substituents on the B atom each have a molecular volume of greater than 250 cubic Å, alternately greater than 300 cubic Å, or alternately greater than 500 cubic Å.

For example, (Ar₃C)_(d) ⁺ can be (Ph₃C)_(d) ⁺, where Ph is a substituted or unsubstituted phenyl, such as substituted with C₁ to C₄₀ hydrocarbyls or substituted C₁ to C₄₀ hydrocarbyls, such as C₁ to C₂₀ alkyls or aromatics or substituted C₁ to C₂₀ alkyls or aromatics.

“Molecular volume” is used herein as an approximation of spatial steric bulk of an activator molecule in solution. Comparison of substituents with differing molecular volumes allows the substituent with the smaller molecular volume to be considered “less bulky” in comparison to the substituent with the larger molecular volume. Conversely, a substituent with a larger molecular volume may be considered “more bulky” than a substituent with a smaller molecular volume.

Molecular volume may be calculated as reported in “A Simple “Back of the Envelope” Method for Estimating the Densities and Molecular Volumes of Liquids and Solids,” Journal of Chemical Education, v. 71(11), November 1994, pp. 962-964, which is incorporated by reference herein. Molecular volume (MV), in units of cubic Å, is calculated using the formula: MV=8.3V_(S), where V_(S) is the scaled volume. V_(S) is the sum of the relative volumes of the constituent atoms, and is calculated from the molecular formula of the substituent using the following table of relative volumes. For fused rings, the V_(S) is decreased by 7.5% per fused ring.

Element Relative Volume H 1 1^(st) short period, Li to F 2 2^(nd) short period, Na to Cl 4 1^(st) long period, K to Br 5 2^(nd) long period, Rb to I 7.5 3^(rd) long period, Cs to Bi 9

For a list of suitable bulky activators please see U.S. Pat. No. 8,658,556, which is incorporated by reference herein.

In another embodiment, one or more of the NCA activators is chosen from the activators described in U.S. Pat. No. 6,211,105.

In at least one embodiment, the activator is selected from one or more of a triaryl carbenium (such as triphenylcarbenium tetraphenylborate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate).

In another embodiment, the activator is selected from one or more of trialkylammonium tetrakis(pentafluorophenyl)borate, N,N-dialkylanilinium tetrakis(pentafluorophenyl)borate, dioctadecylmethylammonium tetrakis(pentafluorophenyl)borate, dioctadecylmethylammonium tetrakis(perfluoronaphthyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis(pentafluorophenyl)borate, trialkylammonium tetrakis-(2,3,4,6-tetrafluorophenyl) borate, N,N-dialkylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, trialkylammonium tetrakis(perfluoronaphthyl)borate, N,N-dialkylanilinium tetrakis(perfluoronaphthyl)borate, trialkylammonium tetrakis(perfluorobiphenyl)borate, N,N-dialkylanilinium tetrakis(perfluorobiphenyl)borate, trialkylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dialkylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dialkyl-(2,4,6-trimethylanilinium) tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, di-(i-propyl)ammonium tetrakis(pentafluorophenyl)borate, (where alkyl is methyl, ethyl, propyl, n-butyl, sec-butyl, or t-butyl).

Suitable activator-to-catalyst ratio, e.g., all NCA activators-to-catalyst ratio may be about a 1:1 molar ratio. Alternate ranges include from 0.1:1 to 100:1, alternately from 0.5:1 to 200:1, alternately from 1:1 to 500:1, alternately from 1:1 to 1000:1. A particularly useful range is from 0.5:1 to 10:1, such as 1:1 to 5:1.

It is also within the scope of the present disclosure that the catalyst compounds can be combined with combinations of alumoxanes and NCA's (see for example, U.S. Pat. Nos. 5,153,157; 5,453,410; EP 0 573 120 B1; WO 1994/007928; and WO 1995/014044 which discuss the use of an alumoxane in combination with an ionizing activator).

Useful chain transfer agents can be hydrogen, alkylalumoxanes, a compound represented by the formula AlR₃, ZnR₂ (where each R is, independently, a C₁-C₈ aliphatic radical, such as methyl, ethyl, propyl, butyl, pentyl, hexyl octyl or an isomer thereof) or a combination thereof, such as diethyl zinc, methylalumoxane, trimethylaluminum, triisobutylaluminum, trioctylaluminum, or a combination thereof.

Furthermore, a catalyst system of the present disclosure may include a metal hydrocarbenyl chain transfer agent represented by the formula:

Al(R′)_(3-v)(R″)_(v)

where each R′ can be independently a C₁-C₃₀ hydrocarbyl group, and/or each R″, can be independently a C₄-C₂₀ hydrocarbenyl group having an end-vinyl group; and v can be from 0.1 to 3.

In embodiments of the invention, the activators described herein have a solubility of more than 10 mM (or more than 20 mM, or more than 50 mM) at 25° C. (stirred 2 hours) in methylcyclohexane and/or a solubility of more than 1 mM (or more than 10 mM, or more than 20 mM) at 25° C. (stirred 2 hours) in isohexane.

The present disclosure relates to a catalyst system comprising a metallocene transition metal compound and an activator compound represented by Formula (IA), to the use of such activator compounds for activating a transition metal compound in a catalyst system for polymerizing olefins, and to processes for polymerizing olefins, the process comprising contacting under polymerization conditions one or more olefins with a catalyst system comprising a metallocene transition metal compound and such activator compounds, where aromatic solvents, such as toluene, are absent (e.g. present at zero mol %, alternately present at less than 1 mol %, preferably the catalyst system, the polymerization reaction and/or the polymer produced are free of detectable aromatic hydrocarbon solvent, such as toluene.

The polyalpha-olefins produced herein preferably contain 0 ppm (alternately less than 1 ppm, alternately less than 5 ppm, alternately less than 10 ppm) of aromatic hydrocarbon. Preferably, the polyalpha-olefins produced herein contain 0 ppm (alternately less than 1 ppm, alternately less than 5 ppm, alternately less than 10 ppm) of toluene.

The catalyst systems used herein preferably contain 0 ppm (alternately less than 1 ppm, alternately less than 5 ppm, alternately less than 10 ppm) of aromatic hydrocarbon. Preferably, the catalyst systems used herein contain 0 ppm (alternately less than 1 ppm, alternately less than 5 ppm, alternately less than 10 ppm) of toluene.

Optional Scavengers or Coactivators

In addition to these activator compounds, scavengers or coactivators may be used. Aluminum alkyl or alumoxane compounds which may be utilized as scavengers or coactivators may include, for example, trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, methylalumoxane (MAO), modified methylalumoxane (MMAO), MMAO-3A, and diethyl zinc.

Optional Support Materials

In embodiments herein, the catalyst system may include an inert support material. The supported material can be a porous support material, for example, talc, and inorganic oxides. Other support materials include zeolites, clays, organoclays, or another organic or inorganic support material, or mixtures thereof.

The support material can be an inorganic oxide in a finely divided form. Suitable inorganic oxide materials for use in catalyst systems herein may include groups 2, 4, 13, and 14 metal oxides, such as silica, alumina, and mixtures thereof. Other inorganic oxides that may be employed either alone or in combination with the silica, or alumina can be magnesia, titania, zirconia. Other suitable support materials, however, can be employed, for example, finely divided functionalized polyolefins, such as finely divided polyethylene. Examples of suitable supports may include magnesia, titania, zirconia, montmorillonite, phyllosilicate, zeolites, talc, clays. Also, combinations of these support materials may be used, for example, silica-chromium, silica-alumina, silica-titania. In at least one embodiment, the support material is selected from Al₂O₃, ZrO₂, SiO₂, SiO₂/Al₂O₃, SiO₂/TiO₂, silica clay, silicon oxide/clay, or mixtures thereof.

The support material, such as an inorganic oxide, can have a surface area in the range of from about 10 m²/g to about 700 m²/g, pore volume in the range of from about 0.1 cm³/g to about 4.0 cm³/g and average particle size in the range of from about 5 μm to about 500 μm. The surface area of the support material can be in the range of from about 50 m²/g to about 500 m²/g, pore volume of from about 0.5 cm³/g to about 3.5 cm³/g and average particle size of from about 10 μm to about 200 μm. For example, the surface area of the support material is in the range is from about 100 m²/g to about 400 m²/g, pore volume from about 0.8 cm³/g to about 3.0 cm³/g and average particle size is from about 5 μm to about 100 μm. The average pore size of the support material useful in the present disclosure is in the range of from 10 Å to 1000 Å, such as 50 Å to about 500 Å, and such as 75 Å to about 350 Å. In at least one embodiment, the support material is a high surface area, amorphous silica (surface area=300 m²/gm; pore volume of 1.65 cm³/gm). For example, suitable silicas can be the silicas marketed under the tradenames of DAVISON™ 952 or DAVISON™ 955 by the Davison Chemical Division of W.R. Grace and Company. In other embodiments, DAVISON™ 948 is used. Alternatively, a silica can be ES-70™ silica (PQ Corporation, Malvern, Pa.) that has been calcined, for example (such as at 875° C.).

The support material should be dry, that is, free of absorbed water. Drying of the support material can be effected by heating or calcining at about 100° C. to about 1,000° C., such as at least about 600° C. When the support material is silica, it is heated to at least 200° C., such as about 200° C. to about 850° C., and such as at about 600° C.; and for a time of about 1 minute to about 100 hours, from about 12 hours to about 72 hours, or from about 24 hours to about 60 hours. The calcined support material must have at least some reactive hydroxyl (OH) groups to produce supported catalyst systems of the present disclosure. The calcined support material is then contacted with at least one polymerization catalyst comprising at least one catalyst compound and an activator.

The support material, having reactive surface groups, such as hydroxyl groups, is slurried in a non-polar solvent and the resulting slurry is contacted with a solution of a catalyst compound and an activator. In at least one embodiment, the slurry of the support material is first contacted with the activator for a period of time in the range of from about 0.5 hour to about 24 hours, from about 2 hours to about 16 hours, or from about 4 hours to about 8 hours. The solution of the catalyst compound is then contacted with the isolated support/activator. In at least one embodiment, the supported catalyst system is generated in situ. In alternate embodiment, the slurry of the support material is first contacted with the catalyst compound for a period of time in the range of from about 0.5 hour to about 24 hours, from about 2 hours to about 16 hours, or from about 4 hours to about 8 hours. The slurry of the supported catalyst compound is then contacted with the activator solution.

The mixture of the catalyst, activator and support is heated from about 0° C. to about 70° C., such as from about 23° C. to about 60° C., such as at room temperature. Contact times can be from about 0.5 hours to about 24 hours, such as from about 2 hours to about 16 hours, or from about 4 hours to about 8 hours.

Suitable non-polar solvents are materials in which all of the reactants used herein, e.g., the activator and the catalyst compound, are at least partially soluble and which are liquid at reaction temperatures. Non-polar solvents can be alkanes, such as isopentane, hexane, n-heptane, octane, nonane, and decane, although a variety of other materials including cycloalkanes, such as cyclohexane, aromatics, such as benzene, toluene, and ethylbenzene, may also be employed.

Polymerization Processes

The present disclosure relates to polymerization processes where monomer (e.g., ethylene; propylene), and optionally comonomer, are contacted with a catalyst system including an activator and at least one catalyst compound, as described above. The catalyst compound and activator may be combined in any order. The catalyst compound and activator may be combined prior to contacting with the monomer. Alternatively the catalyst compound and activator may be introduced into the polymerization reactor separately, wherein they subsequently react to form the active catalyst.

Monomers include substituted or unsubstituted C₂ to C₄₀ alpha olefins, such as C₂ to C₂₀ alpha olefins, such as C₂ to C₁₂ alpha olefins, such as ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene and isomers thereof. In at least one embodiment, the monomer includes ethylene and an optional comonomer comprising one or more C₃ to C₄₀ olefins, such as C₄ to C₂₀ olefins, such as C₆ to C₁₂ olefins. The C₃ to C₄₀ olefin monomers may be linear, branched, or cyclic. The C₃ to C₄₀ cyclic olefins may be strained or unstrained, monocyclic or polycyclic, and may optionally include heteroatoms and/or one or more functional groups. In another embodiment, the monomer includes propylene and an optional comonomer comprising one or more ethylene or C₄ to C₄₀ olefins, such as C₄ to C₂₀ olefins, such as C₆ to C₁₂ olefins. The C₄ to C₄₀ olefin monomers may be linear, branched, or cyclic. The C₄ to C₄₀ cyclic olefins may be strained or unstrained, monocyclic or polycyclic, and may optionally include heteroatoms and/or one or more functional groups.

Exemplary C₂ to C₄₀ olefin monomers and optional comonomers may include ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, norbornene, ethylidenenorbornene, vinylnorbornene, norbornadiene, dicyclopentadiene, cyclopentene, cycloheptene, cyclooctene, cyclooctadiene, cyclododecene, 7-oxanorbornene, 7-oxanorbornadiene, substituted derivatives thereof, and isomers thereof, such as hexene, heptene, octene, nonene, decene, dodecene, cyclooctene, 1,5-cyclooctadiene, 1-hydroxy-4-cyclooctene, 1-acetoxy-4-cyclooctene, 5-methylcyclopentene, cyclopentene, dicyclopentadiene, norbornene, norbornadiene, and their respective homologs and derivatives, such as norbornene, norbornadiene, and dicyclopentadiene.

Polymerization processes of the present disclosure can be carried out in any suitable manner. Any suitable suspension, homogeneous, bulk, solution, slurry, or gas phase polymerization process can be used. Such processes can be run in a batch, semi-batch, or continuous mode. Homogeneous polymerization processes and slurry processes can be used. A bulk homogeneous process can be used. Alternately, no solvent or diluent is present or added in the reaction medium, (except for the small amounts used as the carrier for the catalyst system or other additives, or amounts found with the monomer; e.g., propane in propylene). In another embodiment, the process is a slurry process. As used herein, the term “slurry polymerization process” means a polymerization process performed in a hydrocarbon solvent where a supported catalyst is employed and monomers are polymerized on the supported catalyst particles at a temperature that is below the melting point of the polymer produced. At least 95 wt % of polymer products derived from the supported catalyst are in granular form as solid particles (not dissolved in the diluent).

Suitable diluents/solvents for polymerization may include non-coordinating, inert liquids. Examples of diluents/solvents for polymerization may include straight and branched-chain hydrocarbons, such as isobutane, butane, pentane, isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons, such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof, such as can be found commercially (Isopar™); perhalogenated hydrocarbons, such as perfluorinated C₄ to C₁₀ alkanes, chlorobenzene, and aromatic and alkylsubstituted aromatic compounds, such as benzene, toluene, mesitylene, and xylene. Suitable solvents may also include liquid olefins which may act as monomers or comonomers including ethylene, propylene, 1-butene, 1-hexene, 1-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-octene, 1-decene, and mixtures thereof. In at least one embodiment, aliphatic hydrocarbon solvents are used as the solvent, such as isobutane, butane, pentane, isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons, such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof. In another embodiment, the solvent is not aromatic, such as aromatics are present in the solvent at less than 1 wt %, such as less than 0.5 wt %, such as less than 0 wt % based upon the weight of the solvents.

In at least one embodiment, the feed concentration of the monomers and comonomers for the polymerization is 60 vol % solvent or less, such as 40 vol % or less, such as 20 vol % or less, based on the total volume of the feedstream. In at least one embodiment, the polymerization is run in a bulk process.

Polymerizations can be run at any temperature and/or pressure suitable to obtain the desired polymers. Typical temperatures and/or pressures include a temperature in the range of from about 0° C. to about 300° C., such as about 20° C. to about 200° C., such as about 35° C. to about 160° C., such as from about 80° C. to about 160° C., such as from about 90° C. to about 140° C.; and at a pressure in the range of from about 0.35 MPa to about 25 MPa, such as from about 0.45 MPa to about 6 MPa, or from about 0.5 MPa to about 4 MPa.

In a suitable polymerization, the run time of the reaction can be up to 300 minutes, such as from about 5 minutes to 250 minutes, such as from about 10 minutes to 120 minutes, such as from about 20 minutes to 90 minutes, such as from about 30 minutes to 60 minutes. In a continuous process the run time may be the average residence time of the reactor.

In at least one embodiment, hydrogen is present in the polymerization reactor at a partial pressure of 0.001 psig to 50 psig (0.007 kPa to 345 kPa), such as from 0.01 psig to 25 psig (0.07 kPa to 172 kPa), such as from 0.1 psig to 10 psig (0.7 kPa to 70 kPa).

In at least one embodiment, little or no alumoxane is used in the process to produce the polymers. For example, alumoxane can be present at zero mol %, alternately the alumoxane can be present at a molar ratio of aluminum to transition metal less than 500:1, such as less than 300:1, such as less than 100:1, such as less than 1:1.

In at least one embodiment, the polymerization: 1) is conducted at temperatures of 0° C. to 300° C. (such as 25° C. to 250° C., such as 80° C. to 160° C., such as 100° C. to 140° C.); 2) is conducted at a pressure of atmospheric pressure to 10 MPa (such as 0.35 MPa to 10 MPa, such as from 0.45 MPa to 6 MPa, such as from 0.5 MPa to 4 MPa); 3) is conducted in an aliphatic hydrocarbon solvent (such as isobutane, butane, pentane, isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons, such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof; such as where aromatics are present in the solvent at less than 1 wt %, such as less than 0.5 wt %, such as at 0 wt % based upon the weight of the solvents); 4) wherein the catalyst system used in the polymerization comprises less than 0.5 mol %, such as 0 mol % alumoxane, alternately the alumoxane is present at a molar ratio of aluminum to transition metal less than 500:1, such as less than 300:1, such as less than 100:1, such as less than 1:1; 5) the polymerization occurs in one reaction zone; 6) optionally scavengers (such as trialkyl aluminum compounds) are absent (e.g., present at zero mol %, alternately the scavenger is present at a molar ratio of scavenger metal to transition metal of less than 100:1, such as less than 50:1, such as less than 15:1, such as less than 10:1); and 7) optionally hydrogen is present in the polymerization reactor at a partial pressure of 0.001 psig to 50 psig (0.007 kPa to 345 kPa) (such as from 0.01 psig to 25 psig (0.07 kPa to 172 kPa), such as 0.1 psig to 10 psig (0.7 kPa to 70 kPa)). In at least one embodiment, the catalyst system used in the polymerization includes no more than one catalyst compound.

A “reaction zone” also referred to as a “polymerization zone” is a vessel where polymerization takes place, for example a stirred-tank reactor or a loop reactor. When multiple reactors are used in a continuous polymerization process, each reactor is considered as a separate polymerization zone. For a multi-stage polymerization in a batch polymerization, each polymerization stage is considered as a separate polymerization zone. In at least one embodiment, the polymerization occurs in one reaction zone. Room temperature is 23° C. unless otherwise noted.

In at least one embodiment, the present disclosure provides a process for the production of an ethylene based polymer comprising: polymerizing ethylene by contacting the ethylene with the catalyst system of the present disclosure described above in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. to form an ethylene based polymer. In at least one embodiment, hydrogen is present in the polymerization reactor at a partial pressure of from about 5 psig to about 300 psig, such as from about 10 psig to about 250 psig, such as from about 30 psig to about 200 psig, such as from about 40 psig to about 150 psig, such as from about 50 psig to about 100 psig (e.g., 75 psig). In at least one embodiment, the activity of the catalyst is at least 1,000 gP·mmolcat⁻¹·h⁻¹, such as from about 1,000 gP·mmolcat⁻¹·h⁻¹ to 500,000 gP·mmolcat⁻¹·h⁻¹, such as from about 10,000 gP·mmolcat⁻¹·h⁻¹ to 250,000 gP·mmolcat⁻¹·h⁻¹, such as from about 20,000 gP·mmolcat⁻¹·h⁻¹ to 100,000 gP·mmolcat⁻¹·h⁻¹, alternately from about 500,000 gP·mmolcat⁻¹·h⁻¹ to 2,000,000 gP·mmolcat⁻¹·h⁻¹, such as from about 600,000 gP·mmolcat⁻¹·h⁻¹ to 1,500,000 gP·mmolcat⁻¹·h⁻¹, such as from about 800,000 gP·mmolcat⁻¹·h⁻¹ to 1,000,000 gP·mmolcat⁻¹·h⁻¹.

In another embodiment, the present disclosure provides a process for the production of propylene based polymer comprising: polymerizing propylene by contacting the propylene with the catalyst system of the present disclosure described above in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. to form a propylene based polymer. In at least one embodiment, hydrogen is present in the polymerization reactor at a partial pressure from about 10 psig to about 300 psig, such as from about 20 psig to about 250 psig, such as from about 30 psig to about 200 psig, such as from about 40 psig to about 150 psig, such as from about 50 psig to about 100 psig (e.g., 75 psig). In at least one embodiment, the activity of the catalyst is at least 50 gP·mmolcat⁻¹·h⁻¹, such as from 50 gP·mmolcat⁻¹·h⁻¹ to about 500,000 gP·mmolcat⁻¹·h⁻¹, such as from 100 gP·mmolcat⁻¹·h⁻¹ to about 250,000 gP·mmolcat⁻¹·h⁻¹, such as from 150 gP·mmolcat⁻¹·h⁻¹ to about 150,000 gP·mmolcat⁻¹·h⁻¹, alternately from about 500,000 gP·mmolcat⁻¹·h⁻¹ to about 6,000,000 gP·mmolcat⁻¹·h⁻¹, such as from about 750,000 gP·mmolcat⁻¹·h⁻¹ to about 4,000,000 gP·mmolcat⁻¹·h⁻¹, such as from about 1,000,000 gP·mmolcat⁻¹·h⁻¹ to about 2,000,000 gP·mmolcat⁻¹·h⁻¹.

In another embodiment, the present disclosure provides a process for the production of an ethylene alpha-olefin copolymer comprising: polymerizing ethylene and at least one C₃-C₂₀ alpha-olefin by contacting the ethylene and the at least one C₃-C₂₀ alpha-olefin with a catalyst system described above in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. to form an ethylene alpha-olefin copolymer. In at least one embodiment, hydrogen is present in the polymerization reactor at a partial pressure of from about 10 psig to about 300 psig, such as from about 20 psig to about 250 psig, such as from about 30 psig to about 200 psig, such as from about 40 psig to about 150 psig, such as from about 50 psig to about 100 psig (e.g., 75 psig), alternatively from about 150 psig to about 300 psig (e.g., 200 psig). In at least one embodiment, the activity of the catalyst is at least 500 gP·mmolcat⁻¹·h⁻¹, such as from about 500 gP·mmolcat⁻¹·h⁻¹ to about 5,000,000 gP·mmolcat⁻¹·h⁻¹, such as from about 10,000 gP·mmolcat⁻¹·h⁻¹ to about 2,500,000 gP·mmolcat⁻¹·h⁻¹, such as from about 20,000 gP·mmolcat⁻¹·h⁻¹ to about 1,000,000 gP·mmolcat⁻¹·h⁻¹, alternatively from about 5,000,000 gP·mmolcat⁻¹·h⁻¹ to about 8,000,000 gP·mmolcat⁻¹·h⁻¹.

In another embodiment, the present disclosure provides a process for the production of a propylene alpha-olefin copolymer comprising: polymerizing propylene and at least one ethylene and or at least one C₄-C₂₀ alpha-olefin by contacting the propylene and the at least one ethylene and or at least one C₃-C₂₀ alpha-olefin with a catalyst system described above in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. to form an ethylene alpha-olefin copolymer. In at least one embodiment, hydrogen is present in the polymerization reactor at a partial pressure of from about 10 psig to about 300 psig, such as from about 20 psig to about 250 psig, such as from about 30 psig to about 200 psig, such as from about 40 psig to about 150 psig, such as from about 50 psig to about 100 psig (e.g., 75 psig), alternatively from about 150 psig to about 300 psig (e.g., 200 psig). In at least one embodiment, the activity of the catalyst is at least 500 gP·mmolcat⁻¹·h⁻¹, such as from about 500 gP·mmolcat⁻¹·h⁻¹ to about 5,000,000 gP·mmolcat⁻¹·h⁻¹, such as from about 10,000 gP·mmolcat⁻¹·h⁻¹ to about 2,500,000 gP·mmolcat⁻¹·h⁻¹, such as from about 20,000 gP·mmolcat⁻¹·h⁻¹ to about 1,000,000 gP·mmolcat⁻¹·h⁻¹, alternatively from about 5,000,000 gP·mmolcat⁻¹·h⁻¹ to about 8,000,000 gP·mmolcat⁻¹·h⁻¹.

In at least one embodiment, the conversion of olefin monomer is at least 10%, based upon polymer yield and the weight of the monomer entering the reaction zone, such as 20% or more, such as 30% or more, such as 50% or more, such as 80% or more.

In at least one embodiment, little or no alumoxane is used in the process to produce the polymers. For example, alumoxane is present at zero mol %, alternately the alumoxane is present at a molar ratio of aluminum to transition metal less than 500:1, such as less than 300:1, such as less than 100:1, such as less than 1:1.

In at least one embodiment, little or no scavenger is used in the process to produce the ethylene polymer. For example, scavenger (such as tri alkyl aluminum) is present at zero mol %, alternately the scavenger is present at a molar ratio of scavenger metal to transition metal of less than 100:1, such as less than 50:1, such as less than 15:1, such as less than 10:1.

Other additives may also be used in the polymerization, as desired, such as one or more scavengers, hydrogen, aluminum alkyls, or chain transfer agents (such as alkylalumoxanes, a compound represented by the formula AlR₃ or ZnR₂ (where each R is, independently, a C₁-C₈ aliphatic radical, such as methyl, ethyl, propyl, butyl, pentyl, hexyl octyl or an isomer thereof) or a combination thereof, such as diethyl zinc, methylalumoxane, trimethylaluminum, triisobutylaluminum, trioctylaluminum, or a combination thereof).

Solution Polymerization

In at least one embodiment, the polymerization process with catalyst compounds of the present disclosure is a solution polymerization process.

A solution polymerization is a polymerization process in which the polymer is dissolved in a liquid polymerization medium, such as an inert solvent or monomer(s) or their blends. A solution polymerization is typically homogeneous. A homogeneous polymerization is one where the polymer product is dissolved in the polymerization medium. Such systems are not turbid as described in J. Vladimir Oliveira, C. Dariva and J. C. Pinto, Ind. Eng, Chem. Res. v. 29, 2000, pg. 4627. Solution polymerization may involve polymerization in a continuous reactor in which the polymer formed, the starting monomer and catalyst materials supplied are agitated to reduce or avoid concentration gradients and in which the monomer acts as a diluent or solvent or in which a hydrocarbon is used as a diluent or solvent. Suitable processes can operate at temperatures from about 0° C. to about 250° C., such as from about 50° C. to about 170° C., such as from about 80° C. to about 150° C., such as from about 100° C. to about 140° C., and/or at pressures of about 0.1 MPa or more, such as 2 MPa or more. The upper pressure limit is not critically constrained but can be about 200 MPa or less, such as 120 MPa or less, such as 30 MPa or less. Temperature control in the reactor can generally be obtained by balancing the heat of polymerization and with reactor cooling by reactor jackets or cooling coils to cool the contents of the reactor, auto refrigeration, pre-chilled feeds, vaporization of liquid medium (diluent, monomers or solvent) or combinations of all three. Adiabatic reactors with pre-chilled feeds can also be used. The purity, type, and amount of solvent can be optimized for the maximum catalyst productivity for a particular type of polymerization. The solvent can be also introduced as a catalyst carrier. The solvent can be introduced as a gas phase or as a liquid phase depending on the pressure and temperature. Advantageously, the solvent can be kept in the liquid phase and introduced as a liquid. Solvent can be introduced in the feed to the polymerization reactors.

A process described herein can be a solution polymerization process that may be performed in a batchwise fashion (e.g., batch; semi-batch) or in a continuous process. Suitable reactors may include tank, loop, and tube designs. In at least one embodiment, the process is performed in a continuous fashion and dual loop reactors in a series configuration are used. In at least one embodiment, the process is performed in a continuous fashion and dual continuous stirred-tank reactors (CSTRs) in a series configuration are used. Furthermore, the process can be performed in a continuous fashion and a tube reactor can be used. In another embodiment, the process is performed in a continuous fashion and one loop reactor and one CSTR are used in a series configuration. The process can also be performed in a batchwise fashion and a single stirred tank reactor can be used.

Polyolefin Products

The present disclosure relates to compositions of matter produced by the methods described herein.

In at least one embodiment, a process described herein produces C₂ to C₂₀ olefin homopolymers (e.g., polyethylene; polypropylene), or C₂ to C₂₀ olefin copolymers (e.g., ethylene-octene, ethylene-propylene) and/or propylene-alpha-olefin copolymers, such as C₃ to C₂₀ copolymers (such as propylene-hexene copolymers or propylene-octene copolymers). In at least one embodiment, a process described herein produces C₃ to C₂₀ isotactic olefin homopolymers, such as isotactic polypropylene, such as highly isotactic polypropylene.

The term “isotactic” is defined as having at least 20% or more isotactic pentads according to analysis by ¹³C NMR. The term “highly isotactic” is defined as having 50% or more isotactic pentads according to analysis by ¹³C NMR.

In at least one embodiment, an ethylene or propylene based polymer (homopolymer) has one or more of: an Mw value of 500 g/mol or greater, such as from about 500 g/mol to about 3,000,000 g/mol, such as from about 25,000 g/mol to about 2,000,000 g/mol, alternately from about 3,000,000 g/mol to about 10,000,000 g/mol, such as from about 5,000,000 g/mol to about 7,500,000 g/mol; an Mn value of 500 g/mol or greater, such as from about 500 g/mol to about 2,000,000 g/mol, such as from about 100,000 g/mol to about 1,200,000 g/mol, alternately from about 2,000,000 g/mol to about 10,000,000 g/mol, such as from about 5,000,000 g/mol to about 7,500,000 g/mol; an Mz value of 500 g/mol or greater, such as from about 500 g/mol to about 10,000,000 g/mol, such as from about 100,000 to about 6,000,000 g/mol, alternately from about 10,000,000 g/mol to about 25,000,000 g/mol.

In at least one embodiment, the ethylene or propylene based polymer has an Mw/Mn (PDI) value of from 1 to 20, such as from 5 to 20, such as from 10 to 20, alternatively from 1 to 5, such as from 1.5 to about 3.

In at least one embodiment, the ethylene or propylene based polymer has a melting point (Tm) of at least 50° C., such as from about 50° C. to about 150° C., such as from about 100° C. to about 140° C., such as from about 120° C. to about 140° C., such as from about 130° C. to about 140° C.

In at least one embodiment, an ethylene or propylene based polymer is an ethylene alpha-olefin copolymer or propylene alpha-olefin copolymer having one or more of: an Mw value of 5,000 g/mol or greater, such as from about 1,000 g/mol to about 3,000,000 g/mol, such as from about 1.00 g/mol to about 500,000 g/mol, such as from about 6,000 g/mol to about 250,000 g/mol, such as from about 7,000 g/mol to about 100,000 g/mol, such as from about 8,000 g/mol to about 50,000 g/mol, alternatively from about 500,000 g/mol to about 3,000,000 g/mol, such as from about 750,000 g/mol to about 2,750,000 g/mol, such as from about 1,000,000 g/mol to about 2,500,000 g/mol, such as from about 1,500,000 g/mol to about 2,000,000 g/mol; an Mn value of 1,000 g/mol or greater, such as from about 1,000 g/mol to about 1,500,000 g/mol, such as from about 1,000 g/mol to about 300,000 g/mol, such as from about 2,500 g/mol to about 200,000 g/mol, such as from about 4,000 g/mol to about 50,000 g/mol, alternatively from about 300,000 g/mol to 2,000,000 g/mol, such as from about 200,000 g/mol to about 1,750,000, such as from about 300,000 g/mol to about 1,500,000 g/mol, such as from about 400,000 g/mol to about 1,250,000 g/mol; an Mz value of 1,000 g/mol or greater, such as from about 1,000 g/mol to about 5,000,000 g/mol, such as from about 1,000 g/mol to about 100,000 g/mol, such as from about 2,500 g/mol to about 75,000 g/mol, such as from about 5,000 g/mol to about 50,000 g/mol, alternatively from about 100,000 g/mol to about 10,000,000 g/mol, such as from about 200,000 g/mol to about 7,500,000 g/mol, such as from about 300,000 g/mol to about 5,000,000 g/mol.

In at least one embodiment, the ethylene alpha-olefin copolymer or propylene alpha-olefin copolymer has a comonomer content of from 0.1 wt % to 50 wt %, such as from 1 wt % to 10 wt %, such as from 5 wt % to 25 wt %, such as from 15 wt % to 35 wt %, such as from 25 wt % to 50 wt %.

In at least one embodiment, the ethylene alpha-olefin copolymer or propylene alpha-olefin copolymer has an Mw/Mn (PDI) value of from 1 to 5, such as from 1 to 4, such as from 1 to 3.

In at least one embodiment, the ethylene alpha-olefin copolymer or propylene alpha-olefin copolymer has a melting point (Tm) of at least 100° C., such as from about 100° C. to about 140° C., such as from about 105° C. to about 130° C., such as from about 115° C. to about 125° C.

Accordingly, the present disclosure can provide highly active catalysts capable of operating at high reactor temperatures while producing polymers with substantially high molecular weights.

GPC 4-D

For purposes of the claims, and unless otherwise indicated, the distribution and the moments of molecular weight (Mw, Mn, Mz, Mw/Mn, etc.), the comonomer content and the branching index (g′) are determined by using a high temperature Gel Permeation Chromatography (Polymer Char GPC-IR) equipped with a multiple-channel band-filter based Infrared detector IR5 with a multiple-channel band filter based infrared detector ensemble IR5 with band region covering from about 2,700 cm⁻¹ to about 3,000 cm⁻¹ (representing saturated C—H stretching vibration), an 18-angle light scattering detector and a viscometer. Three Agilent PLgel 10-μm Mixed-B LS columns are used to provide polymer separation. Reagent grade 1,2,4-trichlorobenzene (TCB) (from Sigma-Aldrich) comprising ˜300 ppm antioxidant BHT can be used as the mobile phase at a nominal flow rate of ˜1.0 mL/min and a nominal injection volume of ˜200 μL. The whole system including transfer lines, columns, and detectors can be contained in an oven maintained at ˜145° C. A given amount of sample can be weighed and sealed in a standard vial with ˜10 μL flow marker (heptane) added thereto. After loading the vial in the auto-sampler, the oligomer or polymer may automatically be dissolved in the instrument with ˜8 mL added TCB solvent at ˜160° C. with continuous shaking. The sample solution concentration can be from ˜0.2 mg/ml to ˜2.0 mg/ml, with lower concentrations used for higher molecular weight samples. The concentration, c, at each point in the chromatogram can be calculated from the baseline-subtracted IR5 broadband signal, I, using the equation: c=αI, where α is the mass constant determined with polyethylene or polypropylene standards. The mass recovery can be calculated from the ratio of the integrated area of the concentration chromatography over elution volume and the injection mass which is equal to the pre-determined concentration multiplied by injection loop volume. The conventional molecular weight (IR MW) is determined by combining universal calibration relationship with the column calibration which is performed with a series of monodispersed polystyrene (PS) standards ranging from 700 to 10M gm/mole. The MW at each elution volume is calculated with following equation:

${\log \mspace{11mu} M} = {\frac{\log \left( {K_{PS}/K} \right)}{\alpha + 1} + {\frac{\alpha_{PS} + 1}{\alpha + 1}\log \mspace{11mu} M_{PS}}}$

where the variables with subscript “PS” stand for polystyrene while those without a subscript are for the test samples. In this method, α_(PS)=0.67 and K_(PS)=0.000175, α and K for other materials are as calculated and published in literature (Sun, T. et al. Macromolecules 2001, v. 34, pg. 6812), except that for purposes of this invention and claims thereto, α=0.695+(0.01*(wt. fraction propylene)) and K=0.000579−(0.0003502*(wt. fraction propylene)) for ethylene-propylene copolymers and ethylene-propylene-diene terpolymers, α=0.705 and K=0.0002288 for linear propylene polymers, α=0.695 and K=0.000181 for linear butene polymers, α is 0.695 and K is 0.000579*(1−0.0087*w2b+0.000018*(w2b){circumflex over ( )}2) for ethylene-butene copolymer where w2b is a bulk weight percent of butene comonomer, α is 0.695 and K is 0.000579*(1−0.0075*w2b) for ethylene-hexene copolymer where w2b is a bulk weight percent of hexene comonomer, α is 0.695 and K is 0.000579*(1−0.0077*w2b) for ethylene-octene copolymer where w2b is a bulk weight percent of octene comonomer, and α=0.695 and K=0.000579 for all other linear ethylene polymers. Concentrations are expressed in g/cm³, molecular weight is expressed in g/mole, and intrinsic viscosity (hence K in the Mark-Houwink equation) is expressed in dL/g unless otherwise noted.

The comonomer composition is determined by the ratio of the IR5 detector intensity corresponding to CH₂ and CH₃ channel calibrated with a series of PE and PP homo/copolymer standards whose nominal value are predetermined by NMR or FTIR. In particular, this provides the methyls per 1,000 total carbons (CH₃/1000TC) as a function of molecular weight. The short-chain branch (SCB) content per 1,000TC (SCB/1000TC) is then computed as a function of molecular weight by applying a chain-end correction to the CH₃/1000TC function, assuming each chain to be linear and terminated by a methyl group at each end. The weight % comonomer is then obtained from the following expression in which f is 0.3, 0.4, 0.6, 0.8, and so on for C₃, C₄, C₆, C₈, and so on co-monomers, respectively:

w2=f*SCB/1000TC.

The bulk composition of the polymer from the GPC-IR and GPC-4D analyses is obtained by considering the entire signals of the CH₃ and CH₂ channels between the integration limits of the concentration chromatogram. First, the following ratio is obtained:

${{Bulk}\mspace{14mu} {IR}\mspace{14mu} {ratio}} = {\frac{{Area}\mspace{14mu} {of}\mspace{14mu} {CH}_{3}\mspace{14mu} {signal}\mspace{14mu} {within}\mspace{14mu} {integration}\mspace{14mu} {limits}}{{Area}\mspace{14mu} {of}\mspace{14mu} {CH}_{2}\mspace{14mu} {signal}\mspace{14mu} {within}\mspace{14mu} {integration}\mspace{14mu} {limits}}.}$

Then the same calibration of the CH₃ and CH₂ signal ratio, as mentioned previously in obtaining the CH₃/1000TC as a function of molecular weight, is applied to obtain the bulk CH₃/1000TC. A bulk methyl chain ends per 1,000TC (bulk CH₃end/1000TC) is obtained by weight-averaging the chain-end correction over the molecular-weight range. Then,

w2b=f*bulk CH₃/1000TC

bulk SCB/1000TC=bulk CH₃/1000TC−bulk CH₃end/1000TC

and bulk SCB/1000TC is converted to bulk w2 in the same manner as described above.

The LS detector is the 18-angle Wyatt Technology High Temperature DAWN HELEOSII. The LS molecular weight (M) at each point in the chromatogram is determined by analyzing the LS output using the Zimm model for static light scattering (Light Scattering from Polymer Solutions; Huglin, M. B., Ed.; Academic Press, 1972.):

${\frac{K_{o}c}{\Delta {R(\theta)}} = {\frac{1}{{MP}(\theta)} + {2A_{2}c}}}.$

Here, ΔR(θ) is the measured excess Rayleigh scattering intensity at scattering angle θ, c is the polymer concentration determined from the IR5 analysis, A₂ is the second virial coefficient, P(θ) is the form factor for a monodisperse random coil, and K_(o) is the optical constant for the system:

$K_{o} = \frac{4\pi^{2}{n^{2}\left( {d{n/d}c} \right)}^{2}}{\lambda^{4}N_{A}}$

where N_(A) is Avogadro's number, and (dn/dc) is the refractive index increment for the system. The refractive index, n=1.500 for TCB at 145° C. and λ=665 nm. For analyzing polyethylene homopolymers, ethylene-hexene copolymers, and ethylene-octene copolymers, dn/dc=0.1048 ml/mg and A₂=0.0015; for analyzing ethylene-butene copolymers, dn/dc=0.1048*(1−0.00126*w2) ml/mg and A₂=0.0015 where w2 is weight percent butene comonomer.

A high temperature Agilent (or Viscotek Corporation) viscometer, which has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers, is used to determine specific viscosity. One transducer measures the total pressure drop across the detector, and the other, positioned between the two sides of the bridge, measures a differential pressure. The specific viscosity, η_(S), for the solution flowing through the viscometer is calculated from their outputs. The intrinsic viscosity, [η], at each point in the chromatogram is calculated from the equation [η]=η_(S)/c, where c is concentration and is determined from the IR5 broadband channel output. The viscosity MW at each point is calculated as M=K_(PS)M^(α) ^(PS) ⁺¹/[η], where α_(ps) is 0.67 and K_(ps) is 0.000175.

The branching index (g′_(vis)) is calculated using the output of the GPC-IR5-LS-VIS method as follows. The average intrinsic viscosity, [η]_(avg), of the sample is calculated by:

$\lbrack\eta\rbrack_{avg} = \frac{\sum{c_{i}\lbrack\eta\rbrack}_{i}}{\sum c_{i}}$

where the summations are over the chromatographic slices, i, between the integration limits. The branching index g′_(vis) is defined as

${g_{vis}^{\prime} = \frac{\lbrack\eta\rbrack_{avg}}{{KM}_{v}^{\alpha}}},$

where M_(v) is the viscosity-average molecular weight based on molecular weights determined by LS analysis and the K and α are for the reference linear polymer, which are, for purposes of this invention and claims thereto, α=0.700 and K=0.0003931 for ethylene, propylene, diene monomer copolymers, α=0.705 and K=0.0002288 for linear propylene polymers, α=0.695 and K=0.000181 for linear butene polymers, α is 0.695 and K is 0.000579*(1−0.0087*w2b+0.000018*(w2b){circumflex over ( )}2) for ethylene-butene copolymer where w2b is a bulk weight percent of butene comonomer, α is 0.695 and K is 0.000579*(1−0.0075*w2b) for ethylene-hexene copolymer where w2b is a bulk weight percent of hexene comonomer, α is 0.695 and K is 0.000579*(1-0.0077*w2b) for ethylene-octene copolymer where w2b is a bulk weight percent of octene comonomer, and α=0.695 and K=0.000579 for all other linear ethylene polymers. Concentrations are expressed in g/cm³, molecular weight is expressed in g/mole, and intrinsic viscosity (hence K in the Mark-Houwink equation) is expressed in dL/g unless otherwise noted. Calculation of the w2b values is as discussed above.

Blends

In another embodiment, the polymer (such as the polyethylene or polypropylene) produced herein is combined with one or more additional polymers prior to being formed into a film, molded part or other article. Other useful polymers include polyethylene, isotactic polypropylene, highly isotactic polypropylene, syndiotactic polypropylene, random copolymer of propylene and ethylene, and/or butene, and/or hexene, polybutene, ethylene vinyl acetate, LDPE, LLDPE, HDPE, ethylene vinyl acetate, ethylene methyl acrylate, copolymers of acrylic acid, polymethylmethacrylate or any other polymers polymerizable by a high-pressure free radical process, polyvinylchloride, polybutene-1, isotactic polybutene, ABS resins, ethylene-propylene rubber (EPR), vulcanized EPR, EPDM, block copolymer, styrenic block copolymers, polyamides, polycarbonates, PET resins, cross linked polyethylene, copolymers of ethylene and vinyl alcohol (EVOH), polymers of aromatic monomers such as polystyrene, poly-1 esters, polyacetal, polyvinylidine fluoride, polyethylene glycols, and/or polyisobutylene.

In at least one embodiment, the polymer (such as the polyethylene or polypropylene) is present in the above blends, at from 10 wt % to 99 wt %, based upon the weight of the polymers in the blend, such as 20 wt % to 95 wt %, such as at least 30 wt % to 90 wt %, such as at least 40 wt % to 90 wt %, such as at least 50 wt % to 90 wt %, such as at least 60 wt % to 90 wt %, such as at least 70 to 90 wt %.

The blends described above may be produced by mixing the polymers of the present disclosure with one or more polymers (as described above), by connecting reactors together in series to make reactor blends or by using more than one catalyst in the same reactor to produce multiple species of polymer. The polymers can be mixed together prior to being put into the extruder or may be mixed in an extruder.

The blends may be formed using conventional equipment and methods, such as by dry blending the individual components and subsequently melt mixing in a mixer, or by mixing the components together directly in a mixer, such as, for example, a Banbury mixer, a Haake mixer, a Brabender internal mixer, or a single or twin-screw extruder, which may include a compounding extruder and a side-arm extruder used directly downstream of a polymerization process, which may include blending powders or pellets of the resins at the hopper of the film extruder. Additionally, additives may be included in the blend, in one or more components of the blend, and/or in a product formed from the blend, such as a film, as desired. Such additives are well known in the art, and can include, for example: fillers; antioxidants (e.g., hindered phenolics such as IRGANOX™ 1010 or IRGANOX™ 1076 available from Ciba-Geigy); phosphites (e.g., IRGAFOS™ 168 available from Ciba-Geigy); anti-cling additives; tackifiers, such as polybutenes, terpene resins, aliphatic and aromatic hydrocarbon resins, alkali metal and glycerol stearates, and hydrogenated rosins; UV stabilizers; heat stabilizers; anti-blocking agents; release agents; anti-static agents; pigments; colorants; dyes; waxes; silica; fillers; talc.

Films

Any of the foregoing polymers, such as the foregoing polypropylenes or blends thereof, may be used in a variety of end-use applications. Such applications include, for example, mono- or multi-layer blown, extruded, and/or shrink films. These films may be formed by any number of well-known extrusion or coextrusion techniques, such as a blown bubble film processing technique, wherein the composition can be extruded in a molten state through an annular die and then expanded to form a uni-axial or biaxial orientation melt prior to being cooled to form a tubular, blown film, which can then be axially slit and unfolded to form a flat film. Films may be subsequently unoriented, uniaxially oriented, or biaxially oriented to the same or different extents. One or more of the layers of the film may be oriented in the transverse and/or longitudinal directions to the same or different extents. The uniaxially orientation can be accomplished using typical cold drawing or hot drawing methods. Biaxial orientation can be accomplished using tenter frame equipment or a double bubble processes and may occur before or after the individual layers are brought together. For example, a polyethylene layer can be extrusion coated or laminated onto an oriented polypropylene layer or the polyethylene and polypropylene can be coextruded together into a film then oriented. Likewise, oriented polypropylene could be laminated to oriented polyethylene or oriented polyethylene could be coated onto polypropylene then optionally the combination could be oriented even further. For example, the films can be oriented in the Machine Direction (MD) at a ratio of up to 15, such as from about 5 to about 7, and in the Transverse Direction (TD) at a ratio of up to 15, such as from about 7 to about 9. However, in another embodiment the film is oriented to the same extent in both the MD and TD directions.

The films may vary in thickness depending on the intended application; however, films of a thickness from 1 μm to 50 μm can be suitable. Films intended for packaging can be from 10 μm to 50 μm thick. The thickness of the sealing layer can be from 0.2 μm to 50 μm. There may be a sealing layer on both the inner and outer surfaces of the film or the sealing layer may be present on only the inner or the outer surface.

In another embodiment, one or more layers may be modified by corona treatment, electron beam irradiation, gamma irradiation, flame treatment, or microwave. In at least one embodiment, one or both of the surface layers is modified by corona treatment.

Waxes

Polyolefin waxes, such as polyethylene waxes, having low molecular weight of about 250 g/mol to about 5,000 g/mol, for example, can be prepared in a solution polymerization process using the Lewis base catalysts. The production of polyolefin waxes may be performed at a temperature of from about 50° C. to about 220° C., such as from about 100° C. to about 200° C., such as from about 120° C. to about 160° C. The production of polyolefin waxes may be performed at a reactor pressure of from about 0.5 MPa to about 25 MPa, such as from about 0.7 MPa to about 6 MPa. The production of polyolefin waxes may be performed in the presence of added hydrogen at a partial pressure of from 0 psig to about 100 psig, such as from 0 psig to about 40 psig, such as 0 psig.

Aspects Listing

The present disclosure provides, among others, the following aspects, each of which may be considered as optionally including any alternate aspects.

Clause 1. A catalyst compound represented by Formula (I):

wherein:

M is a group 3, 4, or 5 metal;

each A¹, A², A³, and A⁴ is independently an aromatic group;

J is a heterocyclic Lewis base;

each Q¹ and Q² are independently selected from O, S, N(R³⁰), or P(R³⁰), wherein R³⁰ is C₁-C₄₀ hydrocarbyl, substituted C₁-C₄₀ hydrocarbyl, or a heteroatom, or a heteroatom-containing group;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand,

wherein the ring formed by M, Q¹, A³, A¹, and J is an eight-membered ring and the ring formed by M, Q², A⁴, A² and, J is an eight-membered ring.

Clause 2. A catalyst compound of clause 1, wherein the complex is represented by Formula (II):

wherein:

M is a group 3, 4, or 5 metal;

A¹ and A² are independently an aromatic group;

J is a heterocyclic ring having 5 ring atoms;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms, and where substitutions on the ring can join to form additional rings;

any two L groups may be joined together to form a bidentate Lewis base;

an X group may be joined to an L group to form a monoanionic bidentate group; and

any two X groups may be joined together to form a dianionic ligand,

wherein the ring formed by M, O, A¹, J is an eight-membered ring and the ring formed by M, O, A², and J is an eight-membered ring.

Clause 3. The catalyst compound of clauses 1 or 2, wherein A¹ is represented by the formula:

wherein

indicates a connection to the catalyst compound, and

each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.

Clause 4. The catalyst compound of any of clauses 1 to 3, wherein A² is represented by the formula:

wherein

indicates a connection to the catalyst compound, and

each of R¹³, R¹⁴, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.

Clause 5. The catalyst compound of any of clauses 1 to 4, wherein J is a group 15-containing heterocycle, or a group 16-containing heterocycle. Clause 6. The catalyst compound of any of clauses 1 to 5, wherein J is a nitrogen-containing heterocycle, an oxygen-containing heterocycle, a phosphorus-containing heterocycle, or a sulfur-containing heterocycle. Clause 7. The catalyst compound of any of clauses 1 to 6, wherein J is selected from a thiazole, an oxazole, an oxazoline, an imidazole, a furan, or a thiofuran. Clause 8. The catalyst compound of any of clauses 1 to 7, wherein J is represented by the formula:

wherein

indicates a connection to the catalyst compound; R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group; E is an unsubstituted heteroatom or substituted heteroatom; and each Z is independently an unsubstituted heteroatom or a substituted heteroatom.

Clause 9. The catalyst compound of any of clauses 1 to 8, wherein the complex is represented by Formula (III):

wherein:

M is a group 3, 4, or 5 metal;

L is a Lewis base;

X is an anionic ligand;

n is 1, 2 or 3;

m is 0, 1, or 2;

n+m is not greater than 4;

J is as defined in clauses 5 to 7;

each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms;

each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms;

each of R¹³, R¹⁴, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms; and

R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom, or a heteroatom-containing group.

Clause 10. The catalyst compound of any of clauses 1 to 9, wherein M is zirconium or hafnium. Clause 11. The catalyst compound of any of clauses 1 to 10, wherein m=0, n=2, and X is selected from halogens and hydrocarbyl groups containing 1 to 8 carbons. Clause 12. The catalyst compound of any of clauses 1 to 11, wherein R¹⁷ is hydrogen. Clause 13. The catalyst compound of any of clauses 1 to 12, wherein E is selected from (1) sulfur, (2) oxygen, (3) nitrogen N(R¹⁸) wherein R¹⁸ is hydrogen or C₁-C₁₀ hydrocarbyl, substituted C₁-C₁₀ hydrocarbyl, a heteroatom or a heteroatom-containing group, or (4) phosphorus P(R¹⁹) with R¹⁹ is hydrogen or C₁-C₁₀ hydrocarbyl, substituted C₁-C₁₀ hydrocarbyl, a heteroatom, or a heteroatom-containing group. Clause 14. The catalyst compound of any of clauses 1 to 13, wherein E is sulfur. Clause 15. The catalyst compound of any of clauses 1 to 14, wherein each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, R⁸ are independently selected from hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, alkoxy, silyl, amino, aryloxy, halogen, or phosphino, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms. Clause 16. The catalyst compound of any of clauses 1 to 15, wherein R⁴ and R⁵ are independently C₁-C₁₀ alkyl. Clause 17. The catalyst compound of clause 16, wherein R⁴ and R⁵ are tert-butyl. Clause 18. The catalyst compound of any of clauses 1 to 15, wherein R² and R⁷ are independently C₁-C₁₀ alkyl. Clause 19. The catalyst compound of clause 18, wherein R² and R⁷ are methyl. Clause 20. The catalyst compound of any of clauses 1 to 19, wherein each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ is independently hydrogen or C₁-C₁₀ alkyl. Clause 21. The catalyst compound of any of clauses 1 to 20, wherein each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ is independently hydrogen, methyl, ethyl, propyl, isopropyl, phenyl, cyclohexyl, fluoro, chloro, methoxy, ethoxy, phenoxy, or trimethylsilyl. Clause 22. The catalyst compound of any of clauses 1 to 21, wherein R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ are hydrogen. Clause 23. The catalyst compound of any of clauses 1 to 22, wherein n is 2 and each X is independently chloro, benzyl, or methyl. Clause 24. The catalyst compound of any of clauses 1 to 22, wherein n is 2 and each X is benzyl the catalyst compound is selected from:

Clause 25. The catalyst compound of clause 1, wherein the catalyst compound is selected from:

Clause 26. The catalyst compound of clause 1, wherein the catalyst compound is selected from:

Clause 27. A catalyst system comprising an activator and the catalyst compound of any of clauses 1 to 26. Clause 28. The catalyst system of clause 27, further comprising a support material. Clause 29. The catalyst system of clauses 26 or 27, wherein the support material is selected from Al₂O₃, ZrO₂, SiO₂, SiO₂/Al₂O₃, SiO₂/TiO₂, silica clay, silicon oxide/clay, or mixtures thereof. Clause 30. The catalyst system of any of clauses 27 to 29, wherein the activator comprises a non-coordinating anion activator. Clause 31. The catalyst system of any of clauses 27 to 30, wherein the activator is represented by the formula:

(Z)_(d) ⁺(A^(d-))

wherein Z is (L-H) or a reducible Lewis Acid, L is a Lewis base; H is hydrogen; (L-H)+ is a Bronsted acid; Ad- is a non-coordinating anion having the charge d−; and d is an integer from 1 to 3. Clause 32. The catalyst system of any of clauses 27 to 30, wherein the activator is represented by the formula:

(Z)d+(Ad−)

wherein Ad- is a non-coordinating anion having the charge d−; d is an integer from 1 to 3, and Z is a reducible Lewis acid represented by the formula: (Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl, or a substituted C₁ to C₄₀ hydrocarbyl. Clause 33. The catalyst system of any of clauses 27 to 32, wherein the activator is one or more of:

-   N-methyl-4-nonadecyl-N-octadecylanilinium     tetrakis(perfluoronaphthalen-2-yl)borate, -   N-methyl-4-nonadecyl-N-octadecylanilinium     tetrakis(perfluorophenyl)borate, -   dioctadecylmethylammonium tetrakis(pentafluorophenyl)borate, -   dioctadecylmethylammonium tetrakis(perfluoronaphthyl)borate, -   N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, -   triphenylcarbenium tetrakis(pentafluorophenyl)borate, -   trimethylammonium tetrakis(perfluoronaphthyl)borate, -   triethylammonium tetrakis(perfluoronaphthyl)borate, -   tripropylammonium tetrakis(perfluoronaphthyl)borate, -   tri(n-butyl)ammonium tetrakis(perfluoronaphthyl)borate, -   tri(t-butyl)ammonium tetrakis(perfluoronaphthyl)borate, -   N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate, -   N,N-diethylanilinium tetrakis(perfluoronaphthyl)borate, -   N,N-dimethyl-(2,4,6-trimethylanilinium)     tetrakis(perfluoronaphthyl)borate, -   tropillium tetrakis(perfluoronaphthyl)borate, -   triphenylcarbenium tetrakis(perfluoronaphthyl)borate, -   triphenylphosphonium tetrakis(perfluoronaphthyl)borate, -   triethylsilylium tetrakis(perfluoronaphthyl)borate, -   benzene(diazonium) tetrakis(perfluoronaphthyl)borate, -   trimethylammonium tetrakis(perfluorobiphenyl)borate, -   triethylammonium tetrakis(perfluorobiphenyl)borate, -   tripropylammonium tetrakis(perfluorobiphenyl)borate, -   tri(n-butyl)ammonium tetrakis(perfluorobiphenyl)borate, -   tri(t-butyl)ammonium tetrakis(perfluorobiphenyl)borate, -   N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, -   N,N-diethylanilinium tetrakis(perfluorobiphenyl)borate, -   N,N-dimethyl-(2,4,6-trimethylanilinium)     tetrakis(perfluorobiphenyl)borate, -   tropillium tetrakis(perfluorobiphenyl)borate, -   triphenylcarbenium tetrakis(perfluorobiphenyl)borate, -   triphenylphosphonium tetrakis(perfluorobiphenyl)borate, -   triethylsilylium tetrakis(perfluorobiphenyl)borate, -   benzene(diazonium) tetrakis(perfluorobiphenyl)borate, -   [4-t-butyl-PhNMe₂H][(C₆F₃(C₆F₅)₂)₄B], -   trimethylammonium tetraphenylborate, -   triethylammonium tetraphenylborate, -   tripropylammonium tetraphenylborate, -   tri(n-butyl)ammonium tetraphenylborate, -   tri(t-butyl)ammonium tetraphenylborate, -   N,N-dimethylanilinium tetraphenylborate, -   N,N-diethylanilinium tetraphenylborate, -   N,N-dimethyl-(2,4,6-trimethylanilinium) tetraphenylborate, -   tropillium tetraphenylborate, -   triphenylcarbenium tetraphenylborate, -   triphenylphosphonium tetraphenylborate, -   triethylsilylium tetraphenylborate, -   benzene(diazonium)tetraphenylborate, -   trimethylammonium tetrakis(pentafluorophenyl)borate, -   triethylammonium tetrakis(pentafluorophenyl)borate, -   tripropylammonium tetrakis(pentafluorophenyl)borate, -   tri(n-butyl)ammonium tetrakis(pentafluorophenyl)borate, -   tri(sec-butyl)ammonium tetrakis(pentafluorophenyl)borate, -   N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, -   N,N-diethylanilinium tetrakis(pentafluorophenyl)borate, -   N,N-dimethyl-(2,4,6-trimethylanilinium)     tetrakis(pentafluorophenyl)borate, -   tropillium tetrakis(pentafluorophenyl)borate, -   triphenylcarbenium tetrakis(pentafluorophenyl)borate, -   triphenylphosphonium tetrakis(pentafluorophenyl)borate, -   triethylsilylium tetrakis(pentafluorophenyl)borate, -   benzene(diazonium) tetrakis(pentafluorophenyl)borate, -   trimethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl) borate, -   triethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   tripropylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   tri(n-butyl)ammonium tetrakis-(2,3,4,6-tetrafluoro-phenyl)borate, -   dimethyl(t-butyl)ammonium     tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   N,N-dimethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   N,N-diethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   N,N-dimethyl-(2,4,6-trimethylanilinium)     tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   tropillium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   triphenylcarbenium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   triphenylphosphonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   triethylsilylium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   benzene(diazonium) tetrakis-(2,3,4,6-tetrafluorophenyl)borate, -   trimethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   triethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   tripropylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   tri(n-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   tri(t-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   N,N-dimethylanilinium     tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   N,N-diethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   N,N-dimethyl-(2,4,6-trimethylanilinium)     tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   tropillium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   triphenylphosphonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   triethylsilylium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   benzene(diazonium) tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, -   di-(i-propyl)ammonium tetrakis(pentafluorophenyl)borate, -   dicyclohexylammonium tetrakis(pentafluorophenyl)borate, -   tri(o-tolyl)phosphonium tetrakis(pentafluorophenyl)borate, -   tri(2,6-dimethylphenyl)phosphonium     tetrakis(pentafluorophenyl)borate, -   triphenylcarbenium tetrakis(perfluorophenyl)borate, -   1-(4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluorophenyl)pyrrolidinium, -   tetrakis(pentafluorophenyl)borate, -   4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluoropyridine, and -   triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate).     Clause 34. The catalyst system of any of clauses 27 to 33, further     comprising a metal hydrocarbenyl chain transfer agent represented by     the formula:

Al(R′)_(3-v)(R″)_(v)

wherein each R′ independently is a C₁-C₃₀ hydrocarbyl group; each R″, independently, is a C₄-C₂₀ hydrocarbenyl group having an end-vinyl group; and v is from 0.1 to 3. Clause 35. The catalyst system of any of clauses 27 to 34, wherein the activator comprises an alkylalumoxane. Clause 36. The catalyst system of any of clauses 27 to 35, wherein the alumoxane is present at a molar ratio of aluminum to catalyst compound transition metal of 100:1 or more. Clause 37. A process for the production of an ethylene based polymer comprising: polymerizing ethylene by contacting the ethylene with a catalyst system of any of clauses 27 to 36, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. Clause 38. The process of clause 37, wherein the catalyst has an activity from 1,000 gP·mmolcat⁻¹·h⁻¹ to 500,000 gP·mmolcat⁻¹·h⁻¹. Clause 39. The process of clause 37, wherein the catalyst has an activity from 500,000 gP·mmolcat⁻¹·h⁻¹ to 2,000,000 gP·mmolcat⁻¹·h⁻¹. Clause 40. The process of any of clauses 37 to 39, wherein the ethylene based polymer has an Mw value of from 2,000 to 3,000,000, Mn value of from 1,000 to 2,000,000, Mz value of from 10,000 to 10,000,000, and a PDI of from 1 to 5. Clause 41. The process of any of clauses 37 to 40, wherein the ethylene based polymer has a melting point of from 110° C. to 150° C. Clause 42. A process for the production of a propylene based polymer comprising: polymerizing propylene by contacting the propylene with a catalyst system of any of clauses 27 to 36, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. Clause 43. The process of clause 42, wherein the catalyst has an activity from 50 gP·mmolcat⁻¹·h⁻¹ to 500,000 gP·mmolcat⁻¹·h⁻¹. Clause 44. The process of clause 42, wherein the catalyst has an activity from 500,000 gP·mmolcat⁻¹·h⁻¹ to 6,000,000 gP·mmolcat⁻¹·h⁻¹. Clause 45. The process of any of clauses 42 to 44, wherein the propylene based polymer has an Mw value of from 500 to 15,000, Mn value of from 500 to 15,000, Mz value of from 500 to 20,000, and a PDI of from 1 to 5. Clause 46. The process of any of clauses 42 to 45, wherein the propylene based polymer has a melting point of from 50° C. to 150° C. Clause 47. A process for the production of an ethylene alpha-olefin copolymer comprising: polymerizing ethylene and at least one C₃-C₂₀ alpha-olefin by contacting the ethylene and the at least one C₃-C₂₀ alpha-olefin with a catalyst system of any of clauses 27 to 36, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. Clause 48. The process of clause 47, wherein the catalyst has an activity from 500 gP·mmolcat⁻¹·h⁻¹ to 5,000,000 gP·mmolcat⁻¹·h⁻¹. Clause 49. The process of clause 47, wherein the catalyst has an activity from 5,000,000 gP·mmolcat⁻¹·h⁻¹ to 8,000,000 gP·mmolcat⁻¹·h⁻¹. Clause 50. The process of any of clauses 47 to 49, wherein the ethylene alpha-olefin copolymer has a comonomer content of 0.1 to 50 wt %, an Mw value of from 1,000 to 3,000,000, and Mz value of from 1,000 to 10,000,000, an Mn value of from 1,000 to 1,000,000, and a PDI of from 1 to 5. Clause 51. The process of any of clauses 47 to 50, wherein the ethylene alpha-olefin copolymer has a melting point of from 100° C. to 140° C. Clause 52. A process for the production of a propylene alpha-olefin copolymer comprising: polymerizing propylene and at least one ethylene or at least one C₄-C₂₀ alpha-olefin by contacting the propylene and the at least one ethylene or at least one C₃-C₂₀ alpha-olefin with a catalyst system of any of clauses 27 to 36, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C. Clause 53. The process of clause 52, wherein the catalyst has an activity from 20,000 gP·mmolcat⁻¹·h⁻¹ to 200,000 gP·mmolcat⁻¹·h⁻¹. Clause 54. The process of clause 52, wherein the catalyst has an activity from 100,000 gP·mmolcat⁻¹·h¹ to 5,000,000 gP·mmolcat⁻¹·h⁻¹. Clause 55. The process any of clauses 52 to 54, wherein the propylene alpha-olefin copolymer has a comonomer content of 0.1 to 35 wt %, an Mw value of from 1,000 to 3,000,000, and Mz value of from 1,000 to 10,000,000, an Mn value of from 1,000 to 1,000,000, and a PDI of from 1 to 5. Clause 56. The process any of clauses 52 to 55, wherein the propylene alpha-olefin copolymer has a melting point of from 100° C. to 140° C. Clause 57. A transition metal compound of clause 1 formed by chelation of a tridentate dianionic bis(arylphenolate) heterocyclic ligand to a group 3, 4, or 5 transition metal, where the tridentate ligand coordinates to the metal forming a pair of eight-membered metallocycle rings. Clause 58. The transition metal compound of clause 1, wherein the bis(arylphenolate) heterocyclic ligand is coordinated to the metal center with the formation of a pair of eight-membered metallocycle rings. Clause 59. A transition metal compound of clause 1 formed by chelation of a tridentate dianionic ligand to a group 4 transition metal, where the tridentate ligand coordinates to the metal to form a pair of eight-membered metallocycle rings. Clause 60. A catalyst system comprising an activator and the transition metal compound of clause 59.

EXAMPLES General Considerations for Synthesis:

All reagents were purchased from commercial vendors (Aldrich) and used as received unless otherwise noted. Solvents were sparged with N₂ and dried over 3 Å molecular sieves. All chemical manipulations were performed in a nitrogen environment unless otherwise stated. Flash column chromatography was carried out with Sigma Aldrich silica gel 60 Å (70 Mesh-230 Mesh) using solvent systems specified. NMR spectra were recorded on a Bruker 400 and/or 500 NMR with chemical shifts referenced to residual solvent peaks. All anhydrous solvents were purchased from Fisher Chemical and were degassed and dried over molecular sieves prior to use. Deutrated solvents were purchased from Cambridge Isotope Laboratories and were degassed and dried over molecular sieves prior to use. ¹H NMR spectroscopic data were acquired at 250 MHz, 400 MHz, or 500 MHz using solutions prepared by dissolving approximately 10 mg of a sample in either C₆D₆, CD₂Cl₂, CDCl₃, D₈-toluene, or other deuterated solvent. The chemical shifts (δ) presented are relative to the residual protium in the deuterated solvent at 7.15 ppm, 5.32 ppm, 7.24 ppm, and 2.09 ppm for C₆D₆, CD₂Cl₂, CDCl₃, D₈-toluene, respectively.

Synthesis of Ligands and Catalysts (or Complexes) 1-Bromo-3-(tert-butyl)-2-(methoxymethoxy)-5-methylbenzene

To a solution of 32.8 g (135 mmol) of 2-bromo-6-(tert-butyl)-4-methylphenol in 200 mL of dry THF were added 58.7 mL (337 mmol) of diisopropylethylamine and 25.6 mL (337 mmol) of chloromethyl methyl ether (MOMCl). The reaction mixture was heated for 24 hours at 60° C. and then poured into 1 liter of cold water. The crude product was extracted with 3×200 mL of dichloromethane. The combined organic extract was dried over Na₂SO₄ and evaporated to dryness. Yield 38.7 g (quant.) of a colorless oil. ¹H NMR (CDCl₃, 400 MHz): δ 7.25 (m, 1H), 7.09 (m, 1H), 5.22 (s, 2H), 3.69 (s, 3H), 2.28 (s, 3H), 1.43 (s, 9H).

2-(3′-(tert-Butyl)-2′-(methoxymethoxy)-5′-methyl-[1,1′-biphenyl]-2-yl)-4,4,5,5-tetramethyl-1,3,2-dioxaborolane

To 4.23 g (174 mmol) of a vacuum dried magnesium powder was added 150 mL of dry THF and 10.0 g (34.8 mmol) of 1-bromo-3-(tert-butyl)-2-(methoxymethoxy)-5-methylbenzene. The reaction mixture was stirred overnight at 55° C., then a solution of 6.99 g (36.5 mmol) of 1-bromo-2-chlorobenzene in 100 mL of THF was added dropwise over 3 hours. The resulting suspension was stirred overnight at 55° C., then it was cooled to 0° C. followed by an addition of 9.70 g (52.2 mmol) of 2-isopropoxy-4,4,5,5-tetramethyl-1,3,2-dioxaborolane. The resulting mixture was stirred overnight at room temperature, then poured into 500 mL of water. The crude product was extracted with 3×100 mL of dichloromethane. The combined organic extract was dried over Na₂SO₄ and evaporated to near dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um; eluent: hexane-ethyl acetate=15:1, vol.). Yield 7.20 g (50%) of an yellow oil. ¹H NMR (CDCl₃, 400 MHz): δ 7.75 (dd, J=0.9, 7.4 Hz, 1H), 7.49-7.20 (m, 4H), 7.11 (d, J=1.9 Hz, 1H), 6.85 (d, J=1.7 Hz, 1H), 4.44 (d, J=15.0 Hz, 2H), 3.21 (s, 3H), 2.30 (s, 3H), 1.47 (s, 9H), 1.15 (s, 6H), 1.20 (s, 6H).

2′,2′″-(Thiazole-2,4-diyl)bis(3-(tert-butyl)-5-methyl-[1,1′-biphenyl]-2-ol)

To a solution of 3.37 g (8.23 mmol) of 2-(3′-(tert-butyl)-2′-(methoxymethoxy)-5′-methyl-[1,1′-biphenyl]-2-yl)-4,4,5,5-tetramethyl-1,3,2-dioxaborolane in 70 mL of toluene was added 1.00 g (4.11 mmol) of 2,4-dibromothiazole, 2.18 g (21.0 mmol) of sodium carbonate, 50 mL of water and 10 mL of methanol. The resulting mixture was purged with argon for 10 minutes followed by the addition of 0.47 g (0.41 mmol) of Pd(PPh₃)₄. This mixture was stirred for 12 hours at 90° C., then cooled to room temperature and diluted with 50 mL of water. The obtained mixture was extracted with dichloromethane (3×50 mL), and the combined organic extract was dried over Na₂SO₄ and then evaporated to dryness. To the resulting oil were added 50 mL of THF, 50 mL of methanol and 1 mL of 12N HCl. The reaction mixture was stirred at 60° C. overnight and then poured into 200 mL of water. The obtained mixture was extracted with dichloromethane (3×50 mL), and the combined organic extract was dried over Na₂SO₄ and then evaporated to dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um, eluent: hexane-ethyl acetate=10:1, vol.). Yield 1.20 g (52%) of mixture of two isomers as a white foam. ¹H NMR (CDCl₃, 400 MHz): δ 7.92-8.18 (m, 2H), 7.33-7.50 (m, 6H), 7.00-7.12 (m, 2H), 6.72-6.82 (m, 2H), 6.48-6.53 (m, 1H), 5.30-5.45 (br.s, 2H), 2.22-2.26 (m, 6H), 1.18-1.33 (m, 18H).

Dimethylhafnium[2′,2′″-(thiazole-2,4-diyl)bis(3-(tert-butyl)-5-methyl-[1,1′-biphenyl]-2-olate)] (Catalyst 1)

To a suspension of 285 mg (0.89 mmol) of hafnium tetrachloride in 30 mL of dry toluene was added 1.50 mL (4.00 mmol, 2.7 M) of MeMgBr in diethyl ether in one portion at room temperature. The resulting suspension was stirred for 20 minutes, and a solution of 500 mg (0.89 mmol) of 2′,2′″-(thiazole-2,4-diyl)bis(3-(tert-butyl)-5-methyl-[1,1′-biphenyl]-2-ol) in 10 mL of dry toluene was added dropwise over 5 minutes. The reaction mixture was stirred overnight at room temperature and then evaporated to near dryness. The solids obtained were extracted with 2×20 mL of hot n-hexane, and the combined organic extract was filtered through a thin pad of Celite 503. Next, the filtrate was evaporated to dryness. The resulting solid was washed with 5 mL of n-pentane and then dried in vacuo. Yield 484 mg (71%) of a white solid. Molecular structure of this compound was confirmed by single-crystal X-ray diffraction (FIG. 1). Anal. Calc. for C₃₉H₄₃HfNSO₂: C, 60.97; H, 5.64; N, 1.82. Found: C, 61.32; H, 5.85; N, 1.74. ¹H NMR (CDCl₃, 400 MHz): δ 7.54-7.58 (m, 1H), 7.48-7.52 (m, 1H), 7.35-7.37 (m, 2H), 7.29-7.33 (m, 1H), 7.23-7.27 (m, 1H), 7.05-7.19 (m, 5H), 6.71-6.73 (m, 2H), 2.26 (s, 6H), 1.42 (s, 9H), 1.41 (s, 9H), −0.63 (s, 3H), −0.64 (s, 3H). ¹³C NMR (C₆D₆, 100 MHz): δ 169.02, 158.81, 152.91, 144.08, 138.87, 138.59, 133.75, 133.22, 133.13, 132.37, 132.08, 131.75, 131.27, 129.93, 129.76, 127.96, 127.48, 127.45, 127.37, 127.31, 118.90, 52.27, 52.04, 35.72, 35.68, 30.95, 30.89, 21.35, 21.28.

FIG. 1 shows the molecular structure of Catalyst 1 as determined by single-crystal X-ray diffraction. Hydrogen atoms were omitted and atoms were shown as 50% probability thermal ellipsoids. The sulfur atom (S(2)) was equally disordered in two equivalent positions (the carbon atom C(3) was also disordered, respectively). Selected bond lengths (Å) and angles (degrees): Hf(1)-O(2), 1.9902(18); Hf(1)-O(1), 1.9948(18); Hf(1)-C(40), 2.209(3); Hf(1)-C(39), 2.210(3); Hf(1)-N(1), 2.327(2); O(2)-Hf(1)-O(1), 158.18(7); O(2)-Hf(1)-C(40), 95.87(9); O(1)-Hf(1)-C(40), 98.54(9); O(2)-Hf(1)-C(39), 97.41(9); O(1)-Hf(1)-C(39), 95.32(9); C(40)-Hf(1)-C(39), 102.67(12); O(2)-Hf(1)-N(1), 79.26(7); O(1)-Hf(1)-N(1), 78.95(7); C(40)-Hf(1)-N(1), 128.46(10); C(39)-Hf(1)-N(1), 128.87(10).

2-Methyl-4-phenyl-6H-dibenzo[c,e][1,2]oxaborinin-6-ol

To 2.70 g (111 mmol) of a vacuum dried magnesium powder 150 ml of dry THF and 6.84 g (22.3 mmol) of 1-bromo-3-phenyl-2-(methoxymethoxy)-5-methylbenzene were subsequently added. The reaction mixture was stirred overnight at 55° C., then a solution of 4.35 g (22.7 mmol) of 1-bromo-2-chlorobenzene in 50 ml of THF was added dropwise for 3 hours. The suspension obtained was stirred overnight at 55° C., then it was cooled to 0° C. followed by an addition of 6.22 g (33.4 mmol) of 2-isopropoxy-4,4,5,5-tetramethyl-1,3,2-dioxaborolane. The resulting mixture was stirred overnight at room temperature, then poured into 100 ml of water. The crude product was extracted with 3×100 ml of dichloromethane. The combined organic extract was dried over Na₂SO₄ and then evaporated to near dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um; eluent: hexane-ethyl acetate=10:1, vol.). Yield 3.10 g (46%) of a beige powder. ¹H NMR (CDCl₃, 400 MHz): δ 8.13-8.32 (m, 1H), 7.98-8.13 (m, 1H), 7.95 (dd, J=1.83, 6.04 Hz, 1H), 7.56-7.79 (m, 2H), 7.33-7.50 (m, 4H), 7.21-7.29 (m, 1H), 7.02-7.14 (m, 1H), 4.53 (s, 1H), 2.44-2.54 (m, 3H).

2,2′″-(Thiazole-2,4-diyl)bis(5′-methyl-[1,1′:3′,1″-terphenyl]-2′-ol)

To a solution of 1.66 g (5.81 mmol) of 2-methyl-4-phenyl-6H-dibenzo[c,e][1,2]oxaborinin-6-ol in 16 ml of 1,4-dioxane 640 mg (2.64 mmol) of 2,4-dibromothiazole, 4.30 g (13.2 mmol) of cesium carbonate, and 8 ml of water were subsequently added. The obtained mixture was purged with argon for 10 minutes followed by an addition of 0.30 g (0.26 mmol) of Pd(PPh₃)₄. This mixture was stirred for 12 hours at 90° C., then cooled to room temperature, and diluted with 50 ml of water. The crude product was extracted with dichloromethane (3×50 ml), the combined organic extract was dried over Na₂SO₄ and then evaporated to dryness. The residue was purified by flash chromatography on silica gel 60 (40-63 um, eluent: hexane-ethyl acetate=10:1, vol.). Yield 910 mg (57%) of a mixture of two isomers as a light-yellow foam. ¹H NMR (CDCl₃, 400 MHz): δ 7.91 (d, J=7.4 Hz, 1H), 7.75 (m, 1H), 7.22-7.60 (m, 16H), 7.02-7.15 (m, 2H), 6.92 (m, 2H), 6.79 (s, 1H), 6.30 (br.s, 1H), 6.04-6.17 (m, 1H), 2.28 (br.s, 6H).

(3,5-di-tert-butyl-2-(methoxymethoxy)phenyl)lithium etherate

To a solution of 7.2 g (21.9 mmol) of 1-bromo-3,5-di-tert-butyl-2-(methoxymethoxy)benzene in diethyl ether was added 2.0 mL of an 11.0 M solution of n-butyllithium in hexanes. The reaction was stirred for 30 minutes, then concentrated to remove most of the diethyl ether. The resulting mixture was diluted with pentane and stirred for 10 minutes. The resulting solid was collected by filtration. Yield 7.23 g (71%).

2′-bromo-3,5-di-tert-butyl-2-(methoxymethoxy)-1,1′-biphenyl

To a slurry of 5.10 g (15 mmol) of (3,5-di-tert-butyl-2-(methoxymethoxy)phenyl)lithium etherate in pentane (ca. 50 mL) at 38° C. was added a solution of 2.96 g (15 mmol) of 1-bromo-2-chlorobenzene in 10 mL of pentane, dropwise over 35 minutes. The reaction was stirred at 38° C. for 15 minutes, then filtered to remove all solids. The crude product was purified by chromatography on silica gel, eluted with 5-20% dichloromethane in hexanes. Yield: 4.85 g (78%). ¹H NMR (C₆D₆, 400 MHz): δ 7.59 (d, 1H), 7.49 (d, 1H), 7.28 (m, 2H), 6.91 (t, 1H), 6.73 (t, 1H), 4.67 (d, 1H), 4.55 (d, 1H), 3.02 (s, 1H), 1.61 (s, 9H), 1.29 (s, 9H).

(3′,5′-di-tert-butyl-2′-(methoxymethoxy)-[1,1′-biphenyl]-2-yl)lithium etherate

To a solution of 4.85 g (12 mmol) of 2′-bromo-3,5-di-tert-butyl-2-(methoxymethoxy)-1,1′-biphenyl in 30 mL of diethyl ether was slowly added 1.09 mL of an 11.0 M solution of n-butyllithium in hexanes. The reaction was stirred for 30 minutes, then concentrated to remove most of the diethyl ether. The resulting mixture was diluted with pentane and stirred for 10 minutes. The resulting solid was collected by filtration. Yield 3.22 g (81%).

2′,2′″-(pyrazine-2,6-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-ol)

To 0.746 g (2.13 mmol) of (3′,5′-di-tert-butyl-2′-(methoxymethoxy)-[1,1′-biphenyl]-2-yl)lithium etherate and 0.295 g (2.17 mmol) of zinc chloride was added THF (ca. 20 mL). The resulting mixture was stirred until all solids were dissolved (ca. 10 minutes). To the solution was added 0.350 g (1.06 mmol) of 2,6-diiodopyrazine and 0.044 g (0.05 mmol) of Pd(P(t-Bu)₃)₂. The resulting mixture was stirred overnight at 70° C., then concentrated to remove the THF. The resulting mixture was extracted into dichloromethane and filtered to remove all solids. The filtrate was concentrated to a foam that was mixed with methanol (30 mL) and concentrated HCl (1 mL). The mixture was refluxed for 1 hour, then allowed to cool to ambient temperature. The reaction was concentrated to remove most of the methanol, then diluted with an aqueous solution of NaHCO₃. The crude product was extracted with dichloromethane, and the concentrated extracts were purified by chromatography on silica gel, eluted with 30% dichloromethane and 5% acetone in pentane. Yield 396 mg (59%). ¹H NMR (C₆D₆, 400 MHz): δ 8.24 (s, 1H), 8.20 (s, 1H) 7.40 (d, 2H), 7.20-7.26 (m, 3H), 7.07-7.14 (m, 4H), 6.77 (d, 1H), 6.43 (s, 1H), 5.88 (s, 1H), 1.55 (s, 2H), 1.45 (s, 9H), 1.34 (s, 9H), 1.22 (s, 9H), 1.11 (s, 9H).

2′,2′″-(pyrimidine-2,4-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-ol)

To 1.278 g (3.65 mmol) of (3′,5′-di-tert-butyl-2′-(methoxymethoxy)-[1,1′-biphenyl]-2-yl)lithium etherate and 0.505 g (3.71 mmol) of zinc chloride was added THF (ca. 20 mL). The resulting mixture was stirred until all solids were dissolved (ca. 10 minutes). To the solution was added 0.600 g (1.81 mmol) of 2,6-diiodopyrazine and 0.076 g (0.09 mmol) of Pd(P(t-Bu)₃)₂. The resulting mixture was stirred overnight at 70° C., then concentrated to remove the THF. The resulting mixture was extracted into dichloromethane and filtered to remove all solids. The filtrate was concentrated to a foam that was mixed with methanol (30 mL) and concentrated HCl (1 mL). The mixture was refluxed for 1 hour, then allowed to cool to ambient temperature. The reaction was concentrated to remove most of the methanol, then diluted with an aqueous solution of NaHCO₃. The crude product was extracted with dichloromethane, and the concentrated extracts were purified by chromatography on silica gel, eluted with 30% dichloromethane and 5% acetone in pentane. Yield 480 mg (71%). ¹H NMR (CDCl₃, 400 MHz): δ 7.48-7.55 (m, 8H), 7.43 (m, 2H), 7.37 (d, 2H), 7.11 (d, 2H), 1.48 (s, 18H), 1.35 (s, 18H).

Dimethylhafnium [2,2′″-(thiazole-2,4-diyl)bis(5′-methyl-[1,1′:3′,1″-terphenyl]-2′-olate)] (Catalyst 2)

To a suspension of 160 mg (0.498 mmol) of hafnium tetrachloride in 50 ml of dry toluene 0.77 ml (2.24 mmol, 2.9 M) of MeMgBr in diethyl ether was added in one portion at room temperature. The resulting suspension was stirred for 5 minutes, and a solution of 300 mg (0.498 mmol) of 2,2′″-(thiazole-2,4-diyl)bis(5′-methyl-[1,1′:3′,1″-terphenyl]-2′-ol) in 10 ml of dry toluene was added dropwise for 1 minutes. The reaction mixture was stirred overnight at room temperature and then evaporated to near dryness. The solid obtained was extracted with 2×20 ml of hot toluene, and the combined organic extract was filtered through a thin pad of Celite 503. The filtrate was evaporated to dryness. The resulting solid was washed with 2×5 ml of n-pentane and then dried in vacuo. Yield 261 mg (65%) of a beige solid. Anal. Calc. for C₄₃H₃₅HfNSO₂: C, 63.90; H, 4.36; N, 1.73. Found: C, 64.12; H, 4.55; N, 1.59. ¹H NMR (C₆D₆, 400 MHz): δ 7.79 (d, J=8.4 Hz, 2H), 7.77 (d, J=7.1 Hz, 2H), 7.29-7.33 (m, 4H), 7.27 (d, J=7.6 Hz, 1H), 7.18-7.20 (m, 4H), 7.13-7.15 (m, 5H), 7.08 (dt, J=7.6 Hz, J=1.3 Hz, 1H), 6.95 (dt, J=7.6 Hz, J=1.1 Hz, 1H), 6.88-6.90 (m, 2H), 6.81 (m, 2H), 6.75 (d, J=2.2 Hz, 1H), 5.97 (s, 1H), 2.18 (s, 3H), 2.14 (s, 3H), −0.45 (s, 3H), −0.46 (s, 3H). ¹³C NMR (CDCl₃, 100 MHz): δ 167.10, 155.63, 155.44, 151.57, 142.12, 139.37, 139.14, 131.70, 131.46, 131.15, 131.07, 130.85, 130.65, 130.53, 130.49, 130.17, 129.95, 129.83, 129.67, 129.66, 129.48, 129.07, 128.25, 127.72, 127.67, 127.61, 127.52, 127.29, 127.26, 126.29, 126.24, 125.23, 118.37, 51.25, 51.04, 20.58, 20.55.

Dimethylzirconium [2,2′″-(thiazole-2,4-diyl)bis(5′-methyl-[1,1′:3′,1″-terphenyl]-2′-olate)] (Catalyst 3)

To a suspension of 116 mg (0.498 mmol) of zirconium tetrachloride in 50 ml of dry toluene 0.77 ml (2.24 mmol, 2.9 M) of MeMgBr in diethyl ether was added in one portion at room temperature. The resulting suspension was stirred for 10 seconds, and a solution of 300 mg (0.498 mmol) of 2,2′″-(thiazole-2,4-diyl)bis(5′-methyl-[1,1′:3′,1″-terphenyl]-2′-ol) in 10 ml of dry toluene was added dropwise for 1 minute. The reaction mixture was stirred overnight at room temperature and then evaporated to near dryness. The solid obtained was extracted with 2×20 ml of hot toluene, and the combined organic extract was filtered through a thin pad of Celite 503. The filtrate was evaporated to dryness. The resulting solid was washed with 2×5 ml of n-pentane and then dried in vacuo. Yield 234 mg (65%) of a beige solid. Anal. Calc. for C₄₃H₃₅ZrNSO₂: C, 71.63; H, 4.89; N, 1.94. Found: C, 71.91; H, 4.98; N, 1.75. ¹H NMR (C₆D₆, 400 MHz): δ 7.77-7.80 (m, 4H), 7.27-7.32 (m, 5H), 7.17-7.20 (m, 4H), 7.13 (t, J=7.6 Hz, 1H), 7.08 (t, J=7.7 Hz, 1H), 6.96 (t, J=7.4 Hz, 1H), 6.87-6.92 (m, 2H), 6.80-6.82 (m, 2H), 6.75 (d, J=1.9 Hz, 1H), 5.98 (s, 1H), 2.18 (s, 3H), 2.14 (s, 3H), −0.22 (s, 3H), −0.24 (s, 3H). ¹³C NMR (CDCl₃, 100 MHz): δ 167.08, 155.61, 155.47, 151.55, 142.13, 139.31, 139.19, 131.74, 131.42, 131.15, 130.99, 130.89, 130.68, 130.55, 130.47, 130.14, 129.99, 129.80, 129.69, 129.65, 129.44, 129.02, 128.21, 127.75, 127.63, 127.60, 127.56, 127.27, 127.24, 126.28, 126.21, 125.28, 118.39, 41.17, 40.93, 20.57, 20.54.

Dimethylhafnium[2′,2′″-(pyrazine-2,6-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-olate)] (Catalyst 4)

To a suspension of 47 mg (0.147 mmol) of hafnium tetrachloride in 4 mL of benzene, 0.2 mL of a 3.18 M solution of MeMgBr in diethyl ether was added dropwise at ambient temperature. The resulting mixture was stirred for 10 minutes, and a solution of 94 mg (0.147 mmol) of 2′,2′″-(pyrazine-2,6-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-ol) in 2 mL of benzene was added dropwise. The reaction mixture was stirred for 1 hour at ambient temperature, then concentrated under vacuum. The resulting solid was triturated with pentane, then extracted with hot methylcyclohexane. The combined extracts were filtered through a glass fiber plug. The filtrate was concentrated under vacuum and triturated with pentane to give an orange foam. Yield 82 mg (66%). ¹H NMR (C₆D₆, 400 MHz): δ 8.10 (s, 2H), 7.63 (d, 2H), 7.11 (m, 5H), 6.99 (m, 3H), 6.75 (d, 2H), 1.64 (s, 18H), 1.33 (s, 18H), −0.11 (s, 6H).

Dimethylzirconium[2′,2′″-(pyrazine-2,6-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-olate)] (Catalyst 5)

To a suspension of 33 mg (0.142 mmol) of zirconium tetrachloride in 1.5 mL of toluene at −20° C., 0.2 mL of a 3.0 M solution of MeMgBr in diethyl ether was added dropwise, followed by dropwise addition of a solution of 91 mg (0.142 mmol) of 2′,2′″-(pyrazine-2,6-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-ol) in 3 mL of toluene. The reaction mixture was stirred for 1.5 hours at ambient temperature, then concentrated under vacuum. The resulting solid was extracted with pentane, and the combined extracts were filtered through a glass fiber plug. The filtrate was concentrated under vacuum and triturated with pentane to give an orange foam. Yield 55 mg (51%). ¹H NMR (C₆D₆, 400 MHz): δ 8.06 (s, 2H), 7.61 (s, 2H), 7.11 (m, 5H), 6.96 (m, 3H), 6.72 (s, 2H), 1.66 (s, 18H), 1.32 (s, 18H), 0.12 (s, 6H).

Dimethylzirconium [2′,2′″-(pyrimidine-2,4-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-olate)] (Catalyst 6)

To a suspension of 33 mg (0.142 mmol) of zirconium tetrachloride in 1.5 mL of toluene at −20° C., 0.2 mL of a 3.0 M solution of MeMgBr in diethyl ether was added dropwise, followed by dropwise addition of a solution of 91 mg (0.142 mmol) of 2′,2′″-(pyrimidine-2,4-diyl)bis(3,5-di-tert-butyl-[1,1′-biphenyl]-2-ol) in 3 mL of toluene. The reaction mixture was stirred for 1.5 hours at ambient temperature, then concentrated under vacuum. The resulting solid was extracted with toluene, and the combined extracts were filtered through a glass fiber plug. The filtrate was concentrated under vacuum and triturated with pentane. The resulting solid was washed with pentane (2×1 mL) and dried under vacuum to give a white solid. Yield 66 mg (61%). ¹H NMR (C₆D₆, 400 MHz): δ 7.61 (s, 2H), 7.23 (s, 2H), 7.01-7.10 (m, 8H), 6.80 (t, 2H), 1.73 (s, 18H), 1.32 (s, 18H), 0.57 (s, 6H).

Polymerization Examples

Solvents, polymerization grade toluene and/or isohexanes were supplied by ExxonMobil Chemical Co. and were purified by passing through a series of columns: two 500 cm³ Oxyclear cylinders in series from Labclear (Oakland, Calif.), followed by two 500 cm³ columns in series packed with dried 3 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company), and two 500 cm³ columns in series packed with dried 5 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company).

1-Octene (98%) (Aldrich Chemical Company) was dried by stirring over Na—K alloy overnight followed by filtration through basic alumina (Aldrich Chemical Company, Brockman Basic 1). Tri-(n-octyl)aluminum (TNOA) was purchased from either Aldrich Chemical Company or Akzo Nobel and used as received.

Polymerization grade ethylene was further purified by passing it through a series of columns: 500 cm³ Oxyclear cylinder from Labclear (Oakland, Calif.) followed by a 500 cm³ column packed with dried 3 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company), and a 500 cm³ column packed with dried 5 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company).

Polymerization grade propylene was further purified by passing it through a series of columns: 2250 cm³ Oxiclear cylinder from Labclear followed by a 2250 cm³ column packed with 3 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company), then two 500 cm³ columns in series packed with 5 Å molecular sieves (8 mesh-12 mesh; Aldrich Chemical Company), a 500 cm³ column packed with Selexsorb CD (BASF), and finally a 500 cm³ column packed with Selexsorb COS (BASF).

N,N-Dimethyanilinium tetrakis(pentafluorophenyl)borate, also referred to as Activator 1, was purchased from Albemarle Corporation. Methylalumoxane (MAO), also referred to as Activator 2, was purchased from Albemarle Corporation as a 10 wt % solution in toluene. All complexes and the activators were added to the reactor as dilute solutions in toluene. The concentrations of the solutions of activator, scavenger, and complexes that were added to the reactor were chosen so that between 40 microliters-200 microliters of the solution were added to the reactor to ensure accurate delivery.

Reactor Description and Preparation. Polymerizations were conducted in an inert atmosphere (N₂) drybox using autoclaves equipped with an external heater for temperature control, glass inserts (internal volume of reactor=23.5 mL for C₂ and C₂/C₈ runs; 22.5 mL for C₃ runs), septum inlets, regulated supply of nitrogen, ethylene and propylene, and equipped with disposable polyether ether ketone mechanical stirrers (800 RPM). The autoclaves were prepared by purging with dry nitrogen at 110° C. or 115° C. for 5 hours and then at 25° C. for 5 hours.

Ethylene Polymerization (PE) or Ethylene/1-Octene Copolymerization (EO).

The reactor was prepared as described above, and then purged with ethylene. Toluene (solvent unless stated otherwise), optional 1-octene (0.1 mL when used), and optional MAO were added via syringe at room temperature and atmospheric pressure. The reactor was then brought to process temperature (typically 80° C.) and charged with ethylene to process pressure (typically 75 psig=618.5 kPa or 200 psig=1480.3 kPa) while stirring at 800 RPM. An optional scavenger solution (e.g., TNOA in isohexane) was then added via syringe to the reactor at process conditions. An optional non-coordinating activator (e.g., N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate) solution (in toluene) was added via syringe to the reactor at process conditions, followed by a pre-catalyst (i.e., complex or catalyst) solution (in toluene) via syringe to the reactor at process conditions. Ethylene was allowed to enter (through the use of computer controlled solenoid valves) the autoclaves during polymerization to maintain reactor gauge pressure (+/−2 psi). Reactor temperature was monitored and typically maintained within +/−1° C. Polymerizations were halted by addition of approximately 50 psi O₂/Ar (5 mol % O₂) gas mixture (over the reactor pressure) to the autoclaves for approximately 30 seconds. The polymerizations were quenched after a predetermined cumulative amount of ethylene had been added or for a maximum of 30 minutes polymerization time. The reactors were cooled and vented. The polymer was isolated after the solvent was removed in-vacuo. Yields reported include total weight of polymer and residual catalyst. Catalyst activity is reported as grams of polymer per mmol transition metal compound per hour of reaction time (g/mmol/hr).

Propylene Polymerization.

The reactor was prepared as described above, then heated to 40° C. and purged with propylene gas at atmospheric pressure. Toluene (solvent unless stated otherwise), optional MAO, and liquid propylene (1.0 mL) were added via syringe. The reactor was then heated to process temperature (70° C. or 100° C.) while stirring at 800 RPM. Then optional scavenger solution (e.g., TNOA in isohexane) was added via syringe to the reactor at process conditions. Optional non-coordinating activator (e.g., N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate) solution (in toluene) was then added via syringe to the reactor at process conditions, followed by a pre-catalyst (i.e., complex or catalyst) solution (in toluene) via syringe to the reactor at process conditions. Reactor temperature was monitored and typically maintained within +/−1° C. Polymerizations were halted by addition of approximately 50 psi O₂/Ar (5 mol % O₂) gas mixture (over the reactor pressure) to the autoclaves for approximately 30 seconds. The polymerizations were quenched based on a predetermined pressure loss of approximately 8 psi or for a maximum of 30 minutes polymerization time. The reactors were cooled and vented. The polymer was isolated after the solvent was removed in-vacuo. Yields reported include total weight of polymer and residual catalyst. Catalyst activities are typically reported as grams of polymer per mmol transition metal compound per hour of reaction time (g/mmol/hr).

Polymer Characterization

For analytical testing, polymer sample solutions were prepared by dissolving the polymer in 1,2,4-trichlorobenzene (TCB, 99+% purity from Sigma-Aldrich) containing 2,6-di-tert-butyl-4-methylphenol (BHT, 99% from Aldrich) at 165° C. in a shaker oven for approximately 3 hours. The typical concentration of polymer in solution was between 0.1 mg/mL to 0.9 mg/mL with a BHT concentration of 1.25 mg BHT/mL of TCB. Samples were cooled to 135° C. for testing.

High temperature size exclusion chromatography was performed using an automated “Rapid GPC” system as described in U.S. Pat. Nos. 6,491,816; 6,491,823; 6,475,391; 6,461,515; 6,436,292; 6,406,632; 6,175,409; 6,454,947; 6,260,407; and 6,294,388; each of which is incorporated herein by reference. Molecular weights (weight average molecular weight (Mw) and number average molecular weight (Mn)) and molecular weight distribution (MWD=Mw/Mn), which is also sometimes referred to as the polydispersity (PDI) of the polymer, were measured by Gel Permeation Chromatography using a Symyx Technology GPC equipped with evaporative light scattering detector and calibrated using polystyrene standards (Polymer Laboratories: Polystyrene Calibration Kit S-M-10: Mp (peak Mw) between 5,000 and 3,390,000). Samples (250 μL of a polymer solution in TCB were injected into the system) were run at an eluent flow rate of 2.0 mL/minute (135° C. sample temperatures, 165° C. oven/columns) using three Polymer Laboratories: PLgel 10 μm Mixed-B 300×7.5 mm columns in series. No column spreading corrections were employed. Numerical analyses were performed using Epoch® software available from Symyx Technologies or Automation Studio software available from Freeslate. The molecular weights obtained are relative to linear polystyrene standards.

Differential Scanning Calorimetry (DSC) measurements were performed on a TA-Q 100 instrument to determine the melting point of the polymers. Samples were pre-annealed at 220° C. for 15 minutes and then allowed to cool to room temperature overnight. The samples were then heated to 220° C. at a rate of 100° C./minute and then cooled at a rate of 50° C./minute. Melting points were collected during the heating period.

Samples for infrared analysis were prepared by depositing the stabilized polymer solution onto a silanized wafer (Part number S10860, Symyx). By this method, approximately between 0.12 mg and 0.24 mg of polymer was deposited on the wafer cell. The samples were subsequently analyzed on a Bruker Equinox 55 FTIR spectrometer equipped with Pikes' MappIR specular reflectance sample accessory. Spectra, covering a spectral range of 5,000 cm⁻¹ to 500 cm⁻¹, were collected at a 2 cm⁻¹ resolution with 32 scans.

For ethylene-1-octene copolymers, the wt % copolymer was determined via measurement of the methyl deformation band at ˜1,375 cm⁻¹. The peak height of this band was normalized by the combination and overtone band at −4,321 cm⁻¹, which corrects for path length differences. The normalized peak height was correlated to individual calibration curves from 1H NMR data to predict the wt % copolymer content within a concentration range of ˜2 wt % to 35 wt % for octene. Typically, R² correlations of 0.98 or greater were achieved. Reported values below 4.1 wt % are outside the calibration range.

Tables 1 to 3 illustrate results obtained for Catalyst 1. Catalyst 1 was found to be an active catalyst for olefin polymerization upon activation with N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate (Activator 1) or MAO (Activator 2), respectively.

Table 1 illustrates the ethylene polymerization results obtained using Catalyst 1. General conditions for Runs 1 to 3: catalyst complex=25 nmol, Activator 1=27.5 nmol, ethylene=75 psig, Al(n-octyl)₃=500 nmol, temperature=80° C., total volume=5 mL, solvent=toluene. General conditions for Runs 4 to 6: catalyst complex=25 nmol, Activator 2=0.0125 mmol, ethylene=75 psig, total volume=5 mL, solvent=toluene.

In all cases, narrow PDI values of polyethylenes formed by Catalyst 1 were obtained (e.g., from 1.6 to 3.4). Catalyst 1 was found to be an active catalyst for olefin polymerization upon activation with Activator 1. The polymerization processes were performed using 25 nmol of Catalyst 1 with 1.1 equivalents of Activator 1 in the presence of TNOA as a scavenger. The highest Mw, Mn, Mz, PDI, and Tm values of polyethylenes formed by Catalyst 1 were obtained when Activator 2 was used as the activator for the polymerization (e.g., Runs 4 to 6), when compared to Activator 1 (e.g., Runs 1 to 3).

TABLE 1 Quench Yield Activity Run Catalyst Activator t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 1 Activator 1 79 0.0475 86,582 2 Catalyst 1 Activator 1 70 0.0484 99,566 3 Catalyst 1 Activator 1 81 0.0482 85,689 4 Catalyst 1 Activator 2 310 0.0519 24,108 5 Catalyst 1 Activator 2 422 0.0616 21,020 6 Catalyst 1 Activator 2 405 0.0564 20,053 Mn Mw Mz Tm Run Catalyst Activator (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 1 Activator 1 6,142 10,480 22,004 1.7 122 2 Catalyst 1 Activator 1 4,886 9,159 20,469 1.9 122 3 Catalyst 1 Activator 1 5,889 9,989 21,047 1.7 122 4 Catalyst 1 Activator 2 617,411 1,705,906 4,442,687 2.8 136 5 Catalyst 1 Activator 2 673,104 1,696,005 3,840,668 2.5 136 6 Catalyst 1 Activator 2 1,016,802 1,834,721 4,118,878 1.8 136

Table 2 illustrates the ethylene-octene copolymerization results obtained using Catalyst 1. General conditions for Runs 1 to 5: catalyst complex=25 nmol, Activator 1=27.5 nmol, 0.1 mL octene, Al(n-octyl)₃=500 nmol, temperature=80° C., total volume=5 mL, solvent=toluene. General conditions for Runs 6-10: complex=25 nmol, Activator 2=0.0125 mmol, 0.1 mL octene, temperature=80° C., total volume=5 mL, solvent=toluene. Even though lower catalyst activities of Catalyst 1 were observed when using Activator 2 (e.g., Runs 6 to 10), the highest Mn, Mw, Mz, PDI and Tm values of ethylene-octene copolymers formed by Catalyst 1 were achieved. When using the Activator 1, higher catalyst activities of Catalyst 1 were observed (e.g., Runs 1 to 5), and the lowest Mn, Mw, Mz, PDI and Tm values of ethylene-octene copolymers formed by Catalyst 1 were achieved.

TABLE 2 Pressure Quench Yield Activity Run Catalyst Activator (psig) t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 1 Activator 1 75 93 0.0531 82,219 2 Catalyst 1 Activator 1 75 74 0.0594 115,589 3 Catalyst 1 Activator 1 75 74 0.0571 111,114 4 Catalyst 1 Activator 1 200 32 0.0749 337,050 5 Catalyst 1 Activator 1 200 34 0.0897 379,906 6 Catalyst 1 Activator 2 75 1800 0.0092 736 7 Catalyst 1 Activator 2 75 1800 0.0092 736 8 Catalyst 1 Activator 2 75 1800 0.0095 760 9 Catalyst 1 Activator 2 200 1047 0.0247 3,397 10 Catalyst 1 Activator 2 200 1086 0.0255 3,381 Mn Mw Mz Tm Run Catalyst Activator (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 1 Activator 1 5,043 8,897 17,589 1.8 107 2 Catalyst 1 Activator 1 5,106 8,780 17,688 1.7 110 3 Catalyst 1 Activator 1 4,103 7,673 16,990 1.9 107 4 Catalyst 1 Activator 1 5,133 9,512 21,452 1.9 118 5 Catalyst 1 Activator 1 5,856 9,718 19,576 1.7 118 6 Catalyst 1 Activator 2 7 Catalyst 1 Activator 2 8 Catalyst 1 Activator 2 9 Catalyst 1 Activator 2 538,084 1,230,028 3,150,627 2.3 124 10 Catalyst 1 Activator 2 517,811 1,307,163 4,270,820 2.5 124

Table 3 illustrates the propylene polymerization results obtained using Catalyst 1. General conditions for Runs 1 to 6: catalyst complex=25 nmol, Activator 1=27.5 nmol, propylene=1 mL, Al(n-octyl)₃=500 nmol, total volume=5 mL, solvent=isohexane. General conditions for Runs 7 to 12: catalyst complex=40 nmol, Activator 2=0.025 mmol, propylene=1 mL, total volume=5 mL, solvent=toluene. When using Activator 2 (e.g., Runs 7 to 12), the lowest catalyst activities of Catalyst 1 were observed. Accordingly, the lowest molecular weight polypropylenes were obtained, as well as the lowest Mn, Mz, PDI and Tm values of polypropylenes. Polymerizations using Activator 1 provided higher Mn, Mw, Mz, PDI and Tm values of polypropylenes formed by Catalyst 1. Catalyst 1 exhibited higher catalyst activity when Activator 1 was used as the activator. The polypropylenes formed using Catalyst 1 were obtained with controlled molecular weights and melting points above 120° C.

Altogether, when Catalyst 1 was used for the polymerization and co-polymerization of ethylene (Tables 1 and 2), it was observed that the combination of Catalyst 1 with Activator 1 provided low molecular weight polymers (e.g., from about 7,500 g/mol to about 10,000 g/mol), with a catalyst activity being high (e.g., from about 85,000 gP·mmolcat⁻¹·h⁻¹ to about 380,000 gP·mmolcat⁻¹·h⁻¹). In contrast, when Catalyst 1 was used for the polymerization and co-polymerization of ethylene, it was observed that the combination of Catalyst 1 with Activator 2 provided high molecular weight polymers (e.g., from about 1,200,000 g/mol to about 1,900,000 g/mol), with a catalyst activity being low (e.g., from about 730 gP·mmolcat⁻¹·h⁻¹ to about 25,000 gP·mmolcat⁻¹·h⁻¹). Furthermore, when Catalyst 1 was used for the polymerization of propylene, it was observed that the combination of Catalyst 1 with Activator 1 provided low molecular weight polymers (e.g., from 1,864 g/mol to 2,366 g/mol), with a catalyst activity being high (e.g., from 49,280 gP·mmolcat⁻¹·h⁻¹ to 125,071 gP·mmolcat⁻¹·h⁻¹), whereas the combination of Catalyst 1 with Activator 2 provided low molecular weight polymers (e.g., 1,676 g/mol), with a catalyst activity being low (e.g., from 180 gP·mmolcat⁻¹·h⁻¹ to 505 gP·mmolcat⁻¹·h⁻¹).

TABLE 3 Temperature Quench Yield Activity Run Catalyst Activator (° C.) t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 1 Activator 1 70 257 0.095 53,398 2 Catalyst 1 Activator 1 70 253 0.100 57,031 3 Catalyst 1 Activator 1 70 270 0.092 49,280 4 Catalyst 1 Activator 1 100 140 0.105 108,000 5 Catalyst 1 Activator 1 100 166 0.098 85,186 6 Catalyst 1 Activator 1 100 124 0.108 125,071 7 Catalyst 1 Activator 2 70 1801 0.005 270 8 Catalyst 1 Activator 2 70 1801 0.006 280 9 Catalyst 1 Activator 2 70 1800 0.004 180 10 Catalyst 1 Activator 2 100 1800 0.010 505 11 Catalyst 1 Activator 2 100 1801 0.009 455 12 Catalyst 1 Activator 2 100 1801 0.009 440 Mn Mw Mz Tm Run Catalyst Activator (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 1 Activator 1 1,116 1,864 3,880 1.7 124 2 Catalyst 1 Activator 1 1,254 2,091 3,913 1.7 128 3 Catalyst 1 Activator 1 1,154 1,944 4,059 1.7 126 4 Catalyst 1 Activator 1 1,336 2,331 5,141 1.8 125 5 Catalyst 1 Activator 1 1,244 2,066 3,900 1.7 125 6 Catalyst 1 Activator 1 1,459 2,366 4,228 1.6 125 7 Catalyst 1 Activator 2 8 Catalyst 1 Activator 2 9 Catalyst 1 Activator 2 10 Catalyst 1 Activator 2 1,079 1,676 3,224 1.6 71 11 Catalyst 1 Activator 2 12 Catalyst 1 Activator 2

Tables 4 to 6 illustrate results obtained for Catalysts 4 through 6. Catalysts 4 through 6 were found to be active catalysts for olefin polymerization upon activation with N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate in the presence of the scavenger Al(n-octyl)₃ (Scavenger 1) or bis(diisobutylaluminum) oxide (DIBALO, Scavenger 2), respectively.

Table 4 illustrates the ethylene polymerization results obtained using Catalysts 4 through 6. General conditions: catalyst complex=25 nmol, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate activator=27.5 nmol, ethylene=75 psig, scavenger=500 nmol, temperature=80° C., total volume=5 mL, solvent=toluene. In all cases, narrow PDI values of polyethylenes formed by Catalysts 4, 5, or 6 were obtained (e.g., from 1.6 to 2.8). Higher activities of Catalyst 4 and narrower PDI values of polyethylenes formed by Catalyst 4 were observed when Scavenger 2 was used as the scavenger for polymerization (e.g., Runs 5 to 7), when compared to Scavenger 1 (e.g., Runs 1 to 4).

TABLE 4 Quench Yield Activity Run Catalyst Scavenger t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 4 Scavenger 1 1,234 0.0275 3,209 2 Catalyst 4 Scavenger 1 1,256 0.0315 3,611 3 Catalyst 4 Scavenger 1 1,309 0.0289 3,179 4 Catalyst 4 Scavenger 1 1,234 0.0273 3,186 5 Catalyst 4 Scavenger 2 241 0.0426 25,454 6 Catalyst 4 Scavenger 2 217 0.0374 24,818 7 Catalyst 4 Scavenger 2 253 0.0403 22,938 8 Catalyst 5 Scavenger 1 62 0.0862 200,206 9 Catalyst 5 Scavenger 1 67 0.0835 179,463 10 Catalyst 5 Scavenger 1 50 0.0854 245,952 11 Catalyst 6 Scavenger 1 1,775 0.0269 2,182 12 Catalyst 6 Scavenger 1 1,548 0.0212 1,972 13 Catalyst 6 Scavenger 1 1,800 0.0225 1,800 Mn Mw Mz Tm Run Catalyst Scavenger (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 4 Scavenger 1 195,183 551,048 1,871,576 2.8 137 2 Catalyst 4 Scavenger 1 291,567 832,381 3,260,390 2.9 136 3 Catalyst 4 Scavenger 1 274,018 728,907 2,492,749 2.7 132 4 Catalyst 4 Scavenger 1 221,626 586,904 1,930,878 2.6 134 5 Catalyst 4 Scavenger 2 227,123 450,538 957,638 2.0 128 6 Catalyst 4 Scavenger 2 275,215 504,927 1,118,696 1.8 130 7 Catalyst 4 Scavenger 2 238,686 478,964 1,081,732 2.0 128 8 Catalyst 5 Scavenger 1 193,586 384,953 911,632 2.0 125 9 Catalyst 5 Scavenger 1 216,905 477,030 1,232,310 2.2 128 10 Catalyst 5 Scavenger 1 185,460 382,730 919,513 2.1 125 11 Catalyst 6 Scavenger 1 52,162 98,970 218,297 1.9 136 12 Catalyst 6 Scavenger 1 55,724 102,578 239,356 1.8 135 13 Catalyst 6 Scavenger 1 57,384 91,423 168,728 1.6 135

Table 5 illustrates the ethylene-octene copolymerization results obtained using Catalysts 4 through 6. General conditions: catalyst complex=25 nmol, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate activator=27.5 nmol, 0.1 mL octene, scavenger=500 nmol, temperature=80° C., total volume=5 mL, solvent=toluene.

TABLE 5 Pressure Quench Yield Activity Run Catalyst Scavenger (psig) t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 4 Scavenger 1 75 599 0.0304 7,308 2 Catalyst 4 Scavenger 1 75 378 0.0363 13,829 3 Catalyst 4 Scavenger 1 75 872 0.032 5,284 4 Catalyst 4 Scavenger 1 75 317 0.0357 16,217 5 Catalyst 4 Scavenger 2 75 211 0.0436 29,755 6 Catalyst 4 Scavenger 2 75 163 0.0522 46,115 7 Catalyst 4 Scavenger 2 75 215 0.0442 29,604 8 Catalyst 4 Scavenger 1 200 148 0.0271 26,368 9 Catalyst 4 Scavenger 1 200 101 0.0357 50,899 10 Catalyst 4 Scavenger 1 200 83 0.0347 60,202 11 Catalyst 4 Scavenger 1 200 97 0.0341 50,623 12 Catalyst 4 Scavenger 2 200 83 0.0603 104,617 13 Catalyst 4 Scavenger 2 200 81 0.0613 108,978 14 Catalyst 4 Scavenger 2 200 88 0.0577 94,418 15 Catalyst 5 Scavenger 1 75 49 0.1121 329,437 16 Catalyst 5 Scavenger 1 75 41 0.1283 450,615 17 Catalyst 5 Scavenger 1 75 39 0.1069 394,708 18 Catalyst 5 Scavenger 1 200 25 0.2044 1,177,344 19 Catalyst 5 Scavenger 1 200 25 0.203 1,169,280 20 Catalyst 5 Scavenger 1 200 23 0.2041 1,277,843 21 Catalyst 6 Scavenger 1 75 951 0.0178 2,695 22 Catalyst 6 Scavenger 1 75 1,801 0.0216 1,727 23 Catalyst 6 Scavenger 1 75 1,170 0.0254 3,126 24 Catalyst 6 Scavenger 1 200 627 0.023 5,282 25 Catalyst 6 Scavenger 1 200 570 0.0182 4,598 26 Catalyst 6 Scavenger 1 200 636 0.0212 4,800 Mn Mw Mz Tm Run Catalyst Activator (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 4 Scavenger 1 123,463 256,140 743,878 2.1 118 2 Catalyst 4 Scavenger 1 137,011 284,358 809,583 2.1 117 3 Catalyst 4 Scavenger 1 139,606 294,854 1,000,974 2.1 119 4 Catalyst 4 Scavenger 1 127,953 293,865 1,017,402 2.3 117 5 Catalyst 4 Scavenger 2 114,900 205,477 466,315 1.8 116 6 Catalyst 4 Scavenger 2 104,840 191,621 498,109 1.8 115 7 Catalyst 4 Scavenger 2 109,726 220,408 666,629 2.0 116 8 Catalyst 4 Scavenger 1 159,647 370,676 1,232,782 2.3 123 9 Catalyst 4 Scavenger 1 196,852 411,875 1,388,204 2.1 123 10 Catalyst 4 Scavenger 1 182,792 373,468 969,181 2.0 123 11 Catalyst 4 Scavenger 1 203,559 396,517 1,074,342 1.9 123 12 Catalyst 4 Scavenger 2 157,020 279,832 660,880 1.8 119 13 Catalyst 4 Scavenger 2 156,043 278,674 648,626 1.8 119 14 Catalyst 4 Scavenger 2 158,262 280,182 616,713 1.8 119 15 Catalyst 5 Scavenger 1 50,516 92,167 198,206 1.8 114 16 Catalyst 5 Scavenger 1 42,290 75,471 178,061 1.8 114 17 Catalyst 5 Scavenger 1 55,756 94,933 196,304 1.7 116 18 Catalyst 5 Scavenger 1 56,060 129,720 298,700 2.3 110 19 Catalyst 5 Scavenger 1 77,386 146,450 324,949 1.9 111 20 Catalyst 5 Scavenger 1 75,524 152,542 404,945 2.0 111 21 Catalyst 6 Scavenger 1 51,449 87,243 174,995 1.7 131 22 Catalyst 6 Scavenger 1 56,833 98,418 222,974 1.7 132 23 Catalyst 6 Scavenger 1 55,796 90,622 182,182 1.6 131 24 Catalyst 6 Scavenger 1 61,504 99,163 201,310 1.6 134 25 Catalyst 6 Scavenger 1 56,459 94,430 193,245 1.7 134 26 Catalyst 6 Scavenger 1 65,224 98,883 183,647 1.5 134

Table 6 illustrates the propylene polymerization results obtained using Catalysts 4 through 6. General conditions: catalyst complex=25 nmol, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate activator=27.5 nmol, propylene=1 mL, scavenger=500 nmol, total volume=5 mL, solvent=isohexane.

TABLE 6 Temperature Quench Yield Activity Run Catalyst Scavenger (° C.) t (s) (g) (gP · mmolcat⁻¹ · h⁻¹) 1 Catalyst 4 Scavenger 1 70 1,303 0.0756 8,355 2 Catalyst 4 Scavenger 1 70 847 0.079 13,431 3 Catalyst 4 Scavenger 1 70 590 0.0816 19,916 4 Catalyst 4 Scavenger 2 70 340 0.099 41,929 5 Catalyst 4 Scavenger 2 70 536 0.0839 22,540 6 Catalyst 4 Scavenger 2 70 383 0.0902 33,913 7 Catalyst 4 Scavenger 1 100 220 0.0993 64,996 8 Catalyst 4 Scavenger 1 100 130 0.1344 148,874 9 Catalyst 4 Scavenger 1 100 131 0.1435 157,740 10 Catalyst 4 Scavenger 2 100 1,801 0.0008 64 11 Catalyst 4 Scavenger 2 100 1,800 0.0057 456 12 Catalyst 4 Scavenger 2 100 1,800 0.0043 344 13 Catalyst 5 Scavenger 1 70 213 0.1192 80,586 14 Catalyst 5 Scavenger 1 70 194 0.1337 99,241 15 Catalyst 5 Scavenger 1 70 174 0.1317 108,993 16 Catalyst 5 Scavenger 2 70 108 0.1602 213,600 17 Catalyst 5 Scavenger 2 70 140 0.1327 136,491 18 Catalyst 5 Scavenger 2 70 116 0.1618 200,855 19 Catalyst 5 Scavenger 1 100 1,801 0.0024 192 20 Catalyst 5 Scavenger 1 100 1,801 0.0074 592 21 Catalyst 5 Scavenger 1 100 1,801 0.0059 472 22 Catalyst 6 Scavenger 1 70 1,800 0.0015 120 23 Catalyst 6 Scavenger 1 70 1,800 0.0001 8 24 Catalyst 6 Scavenger 1 70 1,801 0.0008 64 Mn Mw Mz Tm Run Catalyst Activator (g/mol) (g/mol) (g/mol) PDI (° C.) 1 Catalyst 4 Scavenger 1 22,508 92,640 387,960 4.1 147 2 Catalyst 4 Scavenger 1 16,636 76,367 391,943 4.6 145 3 Catalyst 4 Scavenger 1 15,301 70,031 427,961 4.6 144 4 Catalyst 4 Scavenger 2 15,869 28,648 64,071 1.8 143 5 Catalyst 4 Scavenger 2 16,107 26,284 49,735 1.6 142 6 Catalyst 4 Scavenger 2 16,068 27,304 53,027 1.7 142 7 Catalyst 4 Scavenger 1 14,594 23,845 45,629 1.6 141 8 Catalyst 4 Scavenger 1 12,338 22,527 46,796 1.8 140 9 Catalyst 4 Scavenger 1 11,342 22,498 48,390 2.0 140 10 Catalyst 4 Scavenger 2 11 Catalyst 4 Scavenger 2 12 Catalyst 4 Scavenger 2 13 Catalyst 5 Scavenger 1 6,585 25,201 132,277 3.8 136 14 Catalyst 5 Scavenger 1 5,868 11,672 26,210 2.0 133 15 Catalyst 5 Scavenger 1 4,997 11,060 24,957 2.2 132 16 Catalyst 5 Scavenger 2 8,979 17,749 38,245 2.0 130 17 Catalyst 5 Scavenger 2 8,895 18,365 41,002 2.1 130 18 Catalyst 5 Scavenger 2 9,339 17,477 36,137 1.9 129 19 Catalyst 5 Scavenger 1 20 Catalyst 5 Scavenger 1 21 Catalyst 5 Scavenger 1 22 Catalyst 6 Scavenger 1 23 Catalyst 6 Scavenger 1 24 Catalyst 6 Scavenger 1

Overall, catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, or copolymerization as the Lewis base catalysts can be stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers having high molecular weights, polymers having low to very low molecular weights, and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts.

Hence, the present disclosure demonstrates highly active catalysts capable of operating at high reactor temperatures while producing polymers with controlled molecular weights and/or robust isotacticity.

The phrases, unless otherwise specified, “consists essentially of” and “consisting essentially of” do not exclude the presence of other steps, elements, or materials, whether or not, specifically mentioned in this specification, so long as such steps, elements, or materials, do not affect the basic and novel characteristics of the present disclosure, additionally, they do not exclude impurities and variances normally associated with the elements and materials used.

For the sake of brevity, only certain ranges are explicitly disclosed herein. However, ranges from any lower limit may be combined with any upper limit to recite a range not explicitly recited, as well as, ranges from any lower limit may be combined with any other lower limit to recite a range not explicitly recited, in the same way, ranges from any upper limit may be combined with any other upper limit to recite a range not explicitly recited. Additionally, within a range includes every point or individual value between its end points even though not explicitly recited. Thus, every point or individual value may serve as its own lower or upper limit combined with any other point or individual value or any other lower or upper limit, to recite a range not explicitly recited.

All documents described herein are incorporated by reference herein, including any priority documents and/or testing procedures to the extent they are not inconsistent with this text. As is apparent from the foregoing general description and the specific embodiments, while forms of the present disclosure have been illustrated and described, various modifications can be made without departing from the spirit and scope of the present disclosure. Accordingly, it is not intended that the present disclosure be limited thereby. Likewise, the term “comprising” is considered synonymous with the term “including” for purposes of United States law. Likewise whenever a composition, an element or a group of elements is preceded with the transitional phrase “comprising,” it is understood that we also contemplate the same composition or group of elements with transitional phrases “consisting essentially of,” “consisting of,” “selected from the group of consisting of,” or “is” preceding the recitation of the composition, element, or elements and vice versa.

While the present disclosure has been described with respect to a number of embodiments and examples, those skilled in the art, having benefit of this disclosure, will appreciate that other embodiments can be devised which do not depart from the scope and spirit of the present disclosure. 

What is claimed is:
 1. A catalyst compound represented by Formula (I):

wherein: M is a group 3, 4, or 5 metal; each A¹, A², A³, and A⁴ is independently an aromatic group; J is a heterocyclic Lewis base; each Q¹ and Q² are independently selected from O, S, N(R³⁰), or P(R³⁰), wherein R³⁰ is C₁-C₄₀ hydrocarbyl, substituted C₁-C₄₀ hydrocarbyl, or a heteroatom, or a heteroatom-containing group; L is a Lewis base; X is an anionic ligand; n is 1, 2 or 3; m is 0, 1, or 2; n+m is not greater than 4; any two L groups may be joined together to form a bidentate Lewis base; an X group may be joined to an L group to form a monoanionic bidentate group; and any two X groups may be joined together to form a dianionic ligand, wherein the ring formed by M, Q¹, A³, A¹, and J is an eight-membered ring and the ring formed by M, Q², A⁴, A² and, J is an eight-membered ring.
 2. The catalyst compound of claim 1, wherein the complex is represented by Formula (II):

wherein: M is a group 3, 4, or 5 metal; A¹ and A² are independently an aromatic group; J is a heterocyclic ring having 5 ring atoms; L is a Lewis base; X is an anionic ligand; n is 1, 2 or 3; m is 0, 1, or 2; n+m is not greater than 4; each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms, and where substitutions on the ring can join to form additional rings; any two L groups may be joined together to form a bidentate Lewis base; an X group may be joined to an L group to form a monoanionic bidentate group; and any two X groups may be joined together to form a dianionic ligand, wherein the ring formed by M, O, A¹, and J is an eight-membered ring and the ring formed by M, O, A², and J is an eight-membered ring.
 3. The catalyst compound of claim 1, wherein A¹ is represented by the formula:

wherein

indicates a connection to the catalyst compound, and each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.
 4. The catalyst compound of claim 1, wherein A² is represented by the formula:

wherein

indicates a connection to the catalyst compound, and each of R¹³, R¹⁴, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.
 5. The catalyst compound of claim 1, wherein J is a group 15-containing heterocycle, or a group 16-containing heterocycle.
 6. The catalyst compound of claim 1, wherein J is a nitrogen-containing heterocycle, an oxygen-containing heterocycle, a phosphorus-containing heterocycle, or a sulfur-containing heterocycle.
 7. The catalyst compound of any of claims 1 to 6, wherein J is selected from a thiazole, an oxazole, an oxazoline, an imidazole, a furan, or a thiofuran.
 8. The catalyst compound of claim 7, wherein J is represented by the formula:

wherein

indicates a connection to the catalyst compound; R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group; E is unsubstituted heteroatom, or substituted heteroatom; and each Z is independently an unsubstituted heteroatom or a substituted heteroatom.
 9. The catalyst compound of claim 1, wherein the complex is represented by Formula (III):

wherein: each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms; each of R⁹, R¹⁰, R¹¹, and R¹² is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R⁹ and R¹⁰, R¹⁰ and R¹¹, or R¹¹ and R¹² may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms; each of R¹³, R¹⁴, R¹⁵, and R¹⁶ is independently hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group, or one or more of R¹³ and R¹⁴, R¹⁴ and R¹⁵, or R¹⁵ and R¹⁶ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms; R¹⁷ is hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, a heteroatom or a heteroatom-containing group; M is a group 3, 4, or 5 metal; L is a Lewis base; X is an anionic ligand; n is 1, 2 or 3; m is 0, 1, or 2; n+m is not greater than 4; any two L groups may be joined together to form a bidentate Lewis base; an X group may be joined to an L group to form a monoanionic bidentate group; and any two X groups may be joined together to form a dianionic ligand group.
 10. The catalyst compound of claim 9, wherein M is zirconium or hafnium.
 11. The catalyst compound of claim 10, wherein m=0, n=2, and X is selected from halogens or hydrocarbyl groups containing 1 to 8 carbons.
 12. The catalyst compound of claim 11, wherein R¹⁷ is hydrogen.
 13. The catalyst compound of claim 12, wherein E is selected from sulfur or oxygen.
 14. The catalyst compound of claim 13, wherein E is sulfur.
 15. The catalyst compound of any of claim 14, wherein each of R¹, R², R³, R⁴, R⁵, R⁶, R⁷, and R⁸ is independently selected from hydrogen, C₁-C₄₀ hydrocarbyl, C₁-C₄₀ substituted hydrocarbyl, alkoxy, silyl, amino, aryloxy, halogen, or phosphino, or one or more of R¹ and R², R² and R³, R³ and R⁴, R⁵ and R⁶, R⁶ and R⁷, or R⁷ and R⁸ may be joined to form one or more substituted hydrocarbyl rings, unsubstituted hydrocarbyl rings, substituted heterocyclic rings, or unsubstituted heterocyclic rings each having 5, 6, 7, or 8 ring atoms.
 16. The catalyst compound of claim 15, wherein R⁴ and R⁵ are independently C₁-C₁₀ alkyl.
 17. The catalyst compound of claim 16, wherein R⁴ and R⁵ are tert-butyl.
 18. The catalyst compound of claim 15, wherein R² and R⁷ are independently C₁-C₁₀ alkyl.
 19. The catalyst compound of claim 18, wherein R² and R⁷ are methyl.
 20. The catalyst compound of claim 19, wherein each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ is independently hydrogen or C₁-C₁₀ alkyl.
 21. The catalyst compound of claim 19, wherein each of R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ is independently hydrogen, methyl, ethyl, propyl, isopropyl, phenyl, cyclohexyl, fluoro, chloro, methoxy, ethoxy, phenoxy, or trimethylsilyl.
 22. The catalyst compound of claim 21, wherein R¹, R³, R⁶, R⁸, R⁹, R¹⁰, R¹¹, R¹², R¹³, R¹⁴, R¹⁵, R¹⁶, and R¹⁷ are hydrogen.
 23. The catalyst compound of claim 1, wherein n is 2 and each X is independently chloro, benzyl, or methyl.
 24. The catalyst compound of claim 1, wherein the catalyst compound is selected from:


25. The catalyst compound of claim 1, wherein the catalyst compound is selected from:


26. The catalyst compound of claim 1, wherein the catalyst compound is selected from:


27. A catalyst system comprising an activator and the catalyst compound of claim
 1. 28. The catalyst system of claim 27, further comprising a support material.
 29. The catalyst system of claim 28, wherein the support material is selected from Al₂O₃, ZrO₂, SiO₂, SiO₂/Al₂O₃, SiO₂/TiO₂, silica clay, silicon oxide/clay, or mixtures thereof.
 30. The catalyst system of claim 29, wherein the activator comprises a non-coordinating anion activator.
 31. The catalyst system of claim 30, wherein the activator is represented by the formula: (Z)_(d) ⁺(A^(d-)) wherein Z is (L-H) or a reducible Lewis Acid, L is a Lewis base; H is hydrogen; (L-H)⁺ is a Bronsted acid; A^(d-) is a non-coordinating anion having the charge d−; and d is an integer from 1 to
 3. 32. The catalyst system of claim 31, wherein the activator is represented by the formula: (Z)_(d) ⁺(A^(d-)) wherein A^(d-) is a non-coordinating anion having the charge d−; d is an integer from 1 to 3, and Z is a reducible Lewis acid represented by the formula: (Ar₃C⁺), where Ar is aryl or aryl substituted with a heteroatom, a C₁ to C₄₀ hydrocarbyl, or a substituted C₁ to C₄₀ hydrocarbyl.
 33. The catalyst system of claim 30, wherein the activator is one or more of: N-methyl-4-nonadecyl-N-octadecylanilinium tetrakis(perfluoronaphthalen-2-yl)borate, N-methyl-4-nonadecyl-N-octadecylanilinium tetrakis(perfluorophenyl)borate, dioctadecylmethylammonium tetrakis(pentafluorophenyl)borate, dioctadecylmethylammonium tetrakis(perfluoronaphthyl)borate, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, trimethylammonium tetrakis(perfluoronaphthyl)borate, triethylammonium tetrakis(perfluoronaphthyl)borate, tripropylammonium tetrakis(perfluoronaphthyl)borate, tri(n-butyl)ammonium tetrakis(perfluoronaphthyl)borate, tri(t-butyl)ammonium tetrakis(perfluoronaphthyl)borate, N,N-dimethylanilinium tetrakis(perfluoronaphthyl)borate, N,N-diethylanilinium tetrakis(perfluoronaphthyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis(perfluoronaphthyl)borate, tropillium tetrakis(perfluoronaphthyl)borate, triphenylcarbenium tetrakis(perfluoronaphthyl)borate, triphenylphosphonium tetrakis(perfluoronaphthyl)borate, triethylsilylium tetrakis(perfluoronaphthyl)borate, benzene(diazonium) tetrakis(perfluoronaphthyl)borate, trimethylammonium tetrakis(perfluorobiphenyl)borate, triethylammonium tetrakis(perfluorobiphenyl)borate, tripropylammonium tetrakis(perfluorobiphenyl)borate, tri(n-butyl)ammonium tetrakis(perfluorobiphenyl)borate, tri(t-butyl)ammonium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-diethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis(perfluorobiphenyl)borate, tropillium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylphosphonium tetrakis(perfluorobiphenyl)borate, triethylsilylium tetrakis(perfluorobiphenyl)borate, benzene(diazonium) tetrakis(perfluorobiphenyl)borate, [4-t-butyl-PhNMe₂H][(C₆F₃(C₆F₅)₂)₄B], trimethylammonium tetraphenylborate, triethylammonium tetraphenylborate, tripropylammonium tetraphenylborate, tri(n-butyl)ammonium tetraphenylborate, tri(t-butyl)ammonium tetraphenylborate, N,N-dimethylanilinium tetraphenylborate, N,N-diethylanilinium tetraphenylborate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetraphenylborate, tropillium tetraphenylborate, triphenylcarbenium tetraphenylborate, triphenylphosphonium tetraphenylborate, triethylsilylium tetraphenylborate, benzene(diazonium)tetraphenylborate, trimethylammonium tetrakis(pentafluorophenyl)borate, triethylammonium tetrakis(pentafluorophenyl)borate, tripropylammonium tetrakis(pentafluorophenyl)borate, tri(n-butyl)ammonium tetrakis(pentafluorophenyl)borate, tri(sec-butyl)ammonium tetrakis(pentafluorophenyl)borate, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, N,N-diethylanilinium tetrakis(pentafluorophenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis(pentafluorophenyl)borate, tropillium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, triphenylphosphonium tetrakis(pentafluorophenyl)borate, triethylsilylium tetrakis(pentafluorophenyl)borate, benzene(diazonium) tetrakis(pentafluorophenyl)borate, trimethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl) borate, triethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tripropylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tri(n-butyl)ammonium tetrakis-(2,3,4,6-tetrafluoro-phenyl)borate, dimethyl(t-butyl)ammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-diethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tropillium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbenium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylphosphonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triethylsilylium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, benzene(diazonium) tetrakis-(2,3,4,6-tetrafluorophenyl)borate, trimethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tripropylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(n-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(t-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dimethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-diethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tropillium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylphosphonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylsilylium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, benzene(diazonium) tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, di-(i-propyl)ammonium tetrakis(pentafluorophenyl)borate, dicyclohexylammonium tetrakis(pentafluorophenyl)borate, tri(o-tolyl)phosphonium tetrakis(pentafluorophenyl)borate, tri(2,6-dimethylphenyl)phosphonium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(perfluorophenyl)borate, 1-(4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluorophenyl)pyrrolidinium, tetrakis(pentafluorophenyl)borate, 4-(tris(pentafluorophenyl)borate)-2,3,5,6-tetrafluoropyridine, and triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate).
 34. The catalyst system of claim 27, further comprising a metal hydrocarbenyl chain transfer agent represented by the formula: Al(R′)_(3-v)(R″)_(v) wherein each R′ independently is a C₁-C₃₀ hydrocarbyl group; each R″, independently, is a C₄-C₂₀ hydrocarbenyl group having an end-vinyl group; and v is from 0.1 to
 3. 35. The catalyst system of claim 27, wherein the activator comprises an alkylalumoxane.
 36. The catalyst system of claim 35, wherein the alumoxane is present at a molar ratio of aluminum to catalyst compound transition metal of 100:1 or more.
 37. A process for the production of an ethylene based polymer comprising: polymerizing ethylene by contacting the ethylene with a catalyst system of claim 27, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C.
 38. The process of claim 37, wherein the ethylene based polymer has an Mw value of from 2,000 to 3,000,000, Mn value of from 1,000 to 2,000,000, Mz value of from 10,000 to 10,000,000, and a PDI of from 1 to
 5. 39. The process of claim 38, wherein the ethylene based polymer has a melting point of from 110° C. to 150° C.
 40. A process for the production of a propylene based polymer comprising: polymerizing propylene by contacting the propylene with a catalyst system of claim 27, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C.
 41. The process of claim 40, wherein the propylene based polymer has an Mw value of from 500 to 15,000, Mn value of from 500 to 15,000, Mz value of from 500 to 20,000, and a PDI of from 1 to
 5. 42. The process of claim 40, wherein the propylene based polymer has a melting point of from 50° C. to 150° C.
 43. A process for the production of an ethylene alpha-olefin copolymer comprising: polymerizing ethylene and at least one C₃-C₂₀ alpha-olefin by contacting the ethylene and the at least one C₃-C₂₀ alpha-olefin with a catalyst system of claim 27, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C.
 44. The process of claim 43, wherein the ethylene alpha-olefin copolymer has a comonomer content of 0.1 to 50 wt %, an Mw value of from 1,000 to 3,000,000, and Mz value of from 1,000 to 10,000,000, an Mn value of from 1,000 to 1,000,000, and a PDI of from 1 to
 5. 45. The process of claim 43, wherein the ethylene alpha-olefin copolymer has a melting point of from 100° C. to 140° C.
 46. A process for the production of a propylene alpha-olefin copolymer comprising: polymerizing propylene and at least one ethylene or at least one C₄-C₂₀ alpha-olefin by contacting the propylene and the at least one ethylene or at least one C₃-C₂₀ alpha-olefin with a catalyst system of claim 27, in one or more continuous stirred tank reactors or loop reactors, in series or in parallel, at a reactor pressure of from 0.05 MPa to 1,500 MPa and a reactor temperature of from 30° C. to 230° C.
 47. The process of claim 46, wherein the propylene alpha-olefin copolymer has a comonomer content of 0.1 to 35 wt %, an Mw value of from 1,000 to 3,000,000, and Mz value of from 1,000 to 10,000,000, an Mn value of from 1,000 to 1,000,000, and a PDI of from 1 to
 5. 48. The process of claim 46, wherein the propylene alpha-olefin copolymer has a melting point of from 100° C. to 140° C. 